CN211902912U - High-calorific-value dangerous waste treatment system based on plasma treatment - Google Patents
High-calorific-value dangerous waste treatment system based on plasma treatment Download PDFInfo
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Abstract
The utility model provides a dangerous waste treatment system of high calorific value based on plasma handles. The system comprises a conveying unit, a desorption unit, a plasma pyrolysis unit, a dioxin removal unit, a plasma desulfurization and denitrification unit and an ash output unit. According to the invention, the staged cracking is adopted aiming at different component characteristics of the high-calorific-value hazardous waste, the Cl element in the high-calorific-value hazardous waste is removed in the desorption unit, the gasified gas generated by pyrolysis of the plasma pyrolysis furnace and the desorbed gas from the thermal desorption reactor are completely converted into carbon dioxide under the high temperature, high enthalpy and high oxidation activity of oxygen plasma, the generation of a precursor of dioxin is avoided, and the low-temperature plasma reactor is adopted for carrying out high-efficiency desulfurization and denitrification on the flue gas. The utility model discloses can improve the innoxious degree of high calorific value hazardous waste treatment, realize minimizing and resourceization simultaneously.
Description
Technical Field
The utility model belongs to the field of harmless and resourceful treatment of solid hazardous waste, in particular to a method and a system for treating high-calorific-value hazardous waste based on plasma.
Background
The high-calorific-value hazardous waste is numbered as HW12 in national hazardous waste records, belongs to residues and intermediate wastes generated in reactions such as nitration, sulfonation, diazotization, halogenation and the like in dye production, can generate highly toxic substances such as dioxin and the like due to improper treatment, and is black powdery hazardous waste with high calorific value.
At present, the treatment methods for hazardous wastes mainly include landfill methods, solidification methods, biochemical methods, and thermochemical treatment methods. The landfill method has the advantages of wide application, mature technology, large treatment capacity, simple process and low operation and maintenance cost, but the landfill method cannot thoroughly make hazardous wastes harmless, can pollute air, soil and underground water, and percolate generated by landfill anaerobism is difficult to treat and occupies a large amount of land resources. The solidification method is that the dangerous waste and materials such as cement, asphalt and the like are mixed to form a material of a highly impermeable solid matrix, and toxic parts in the dangerous waste are wrapped through physical and chemical changes to play a role of temporary solidification. However, in the case of prolonged sewage erosion and sunlight, the toxic portion of the hazardous waste leaks out of the package, creating secondary pollution. The biochemical treatment is to adopt various bacteria generated in the process of accumulating hazardous wastes so as to carry out harmless treatment on the hazardous wastes under the degradation action of the bacteria. But the biochemical treatment is greatly influenced by water temperature, pH value and the like, the energy consumption is high, the cost is high, side reactions exist, and the biological treatment technology has a long period. The thermochemical treatment mainly comprises two technologies of incineration and pyrolysis gasification. The burning mainly adopts a rotary kiln, materials can be coked in the rotary kiln, the treatment capacity is gradually reduced along with the operation time, a large amount of excess parameters are required to be given in the rotary kiln, the tail gas treatment cost is increased, the burning is just harmless treatment, and the resource recovery cannot be achieved. Although pyrolysis gasification can reduce the operation cost after incineration treatment, the pyrolysis gasification can generate organic pollutants such as dioxin, furan and the like, and huge pollution is caused to the environment.
The high-calorific-value dangerous waste belongs to high-calorific-value dangerous waste, at present, a process of incinerating a plurality of wastes together is adopted, the high-calorific-value dangerous waste contains a large amount of organic matters and is wasted without recycling, dioxin generated in the incineration process is treated by 3T (retention time is more than 2S, temperature is more than 800 ℃, turbulence is good) +1E (enough combustion-supporting air) on the conventional treatment, but the flue gas turbulence is poor, the mixing is not uniform, the treatment effect is not good, and the denitration and desulfurization of the tail gas treatment are treated by SCNR or SCR, the process is complex, and the desulfurization and denitration efficiency is low.
Disclosure of Invention
An object of the utility model is to prior art not enough, provide a dangerous waste treatment system of high calorific value based on plasma handles, improve the innocent treatment degree of the dangerous waste treatment of high calorific value, realize minimizing and resourceization simultaneously.
The utility model provides a dangerous waste treatment system of high calorific value based on plasma is handled, including conveying unit, desorption unit, plasma pyrolysis unit, dioxin deviate from unit, plasma SOx/NOx control unit and lime-ash output unit;
the conveying unit comprises a stirrer, a spiral conveyor communicated with a discharge hole of the stirrer, and an air lock communicated with a discharge hole of the spiral conveyor;
the desorption unit comprises a thermal desorption reactor, a quench tower, an air flotation machine for oil-water separation and an air cooler; the thermal desorption reactor is provided with a heating jacket, a feed inlet of the thermal desorption reactor is communicated with an air lock discharge port in the conveying unit, a desorption gas outlet of the thermal desorption reactor is communicated with an inlet of the quench tower, a cooled liquid phase outlet of the quench tower is communicated with an inlet of the air floatation machine, a purified water outlet after oil-water separation treatment of the air floatation machine is communicated with an inlet of an air cooler, and a cold water outlet of the air cooler is communicated with a cooling water inlet of the quench tower;
the plasma pyrolysis unit comprises a plasma pyrolysis furnace, a plasma power supply, a deionized water air cooler and a nitrogen making machine; the plasma pyrolysis furnace consists of a furnace body and a nitrogen plasma torch which is arranged on the furnace body and is used as a heating heat source, a nitrogen outlet of the nitrogen making machine is connected with the nitrogen plasma torch to provide working medium nitrogen for the nitrogen plasma torch, meanwhile, the nitrogen making machine is communicated with an air flotation machine in a desorption unit to provide a dissolved air source for the air flotation machine and is communicated with an air lock in the desorption unit, the plasma power source is connected with the nitrogen plasma torch to provide a power source for the plasma torch, and the deionized water air cooler is communicated with a water cooling channel arranged on the nitrogen plasma torch to form a circulating water cooling loop so as to cool nitrogen plasma in work; a feed port of the plasma pyrolysis furnace is communicated with a desorption solid phase outlet of a thermal desorption reactor in a desorption unit;
the dioxin extracting unit comprises a plasma gas combustion reactor, a plasma power supply, a deionized water air cooler and a nitrogen making machine, wherein the plasma gas combustion reactor consists of a reaction tank body and an oxygen plasma torch arranged at the top of the tank body, an oxygen outlet of the nitrogen making machine is communicated with the oxygen plasma torch to provide working medium oxygen for the oxygen plasma torch, the plasma power supply is communicated with the oxygen plasma torch to provide a power supply for the oxygen plasma torch, and the deionized water air cooler is communicated with a water cooling channel arranged on the oxygen plasma torch to form a circulating water cooling loop so as to cool the oxygen plasma in working; the gas inlet of the plasma gas combustion reactor is communicated with a gas outlet at the top of the quench tower in the thermal desorption unit and is also communicated with a pyrolysis gas outlet of the plasma pyrolysis furnace, and a flue gas outlet after combustion reaction of the plasma gas combustion reactor is communicated with an inlet of a heating jacket of the thermal desorption reactor in the thermal desorption unit to provide a thermal desorption reaction heat source;
the plasma desulfurization and denitrification unit comprises a dry quenching tower, a bag-type dust collector, a low-temperature plasma reactor, a low-temperature plasma power supply and a deacidification tower; the gas inlet of the dry quenching tower is communicated with the outlet of a heating jacket of the thermal desorption reactor, the outlet of the dry quenching tower is communicated with the inlet of a bag-type dust remover, the outlet of the bag-type dust remover is communicated with the inlet of the low-temperature plasma reactor, an activated carbon injector for injecting activated carbon into a communicating pipeline is arranged on the communicating pipeline, the outlet of the low-temperature plasma reactor is communicated with the gas inlet of the deacidification tower, and the gas outlet of the deacidification tower is communicated with the atmosphere; alkali liquor inlets for denitration and desulfurization are formed in the dry quenching tower and the deacidification tower;
the ash output unit comprises a water quenching box and a slag conveyor, and molten glass liquid pyrolyzed in a plasma pyrolyzing furnace of the plasma pyrolyzing unit is quenched and then is salvaged and recovered by the slag conveyor.
Furthermore, the plasma desulfurization and denitration unit is also provided with an alkali liquor preparation box for preparing a sodium hydroxide solution, an alkali liquor outlet of the alkali liquor preparation box is respectively communicated with alkali liquor inlets of the dry quenching tower and the deacidification tower through an alkali liquor delivery pump, and the alkali liquor is delivered to the dry quenching tower and the deacidification tower to remove residual acid gas in the flue gas.
Further, the plasma SOx/NOx control unit still is provided with the salt storage tank, the liquid phase export of deacidification tower and salt storage tank intercommunication to collect gained salt and surplus alkali lye after the SOx/NOx control, the export of salt storage tank is prepared the case through alkali lye circulating pump and alkali lye and is communicated, realizes the cyclic utilization of alkali lye.
Furthermore, a smoke exhaust fan and a chimney are sequentially arranged at a gas outlet of the deacidification tower, so that the flue gas after desulfurization and denitrification is smoothly discharged.
Further, the plasma desulfurization and denitration unit is also provided with an alcohol storage tank, and the alcohol storage tank is communicated with the low-temperature plasma reactor through an alcohol pump to provide alcohol solution required by the reaction.
Further, the low-temperature plasma reactor is based on a double-acting mechanism of corona discharge and dielectric barrier discharge, a plurality of discharge tips are concentrically arranged at the positive electrode of the reactor in an outer cylinder container, an electric field with extremely high strength can be generated after voltage is applied to the positive electrode, so that corona discharge is generated, gas enters the reactor container and contacts with the discharge tips, nitrogen oxide and sulfide in the gas are rapidly decomposed in a corona area under the action of alcohol substances, the nitrogen oxide is converted into nitrogen, and sulfur dioxide is converted into OHSO2And HSO3. Preferably, the low-temperature plasma reactor structure comprises an electrode as a positive electrode and an outer cylinder as a negative electrode; the outer cylinder body is provided with a gas inlet, a gas outlet and a sewage outlet; the electrode (anode) is uniformly arranged on the wall surface of the outer cylinder along the circumferential direction of the outer cylinder, the part of the electrode positioned in the outer cylinder is a conical electrode tip along the radial direction of the outer cylinder, the adjacent electrode tips are staggered on the radial plane of the outer cylinder, and the mutual staggered angle is 30-90 degrees; the electrode and the outer cylinder are separated by an insulating material, the thickness of the insulating material is more than 20mm, and the insulating material can be high-density polyethylene or PEK or ceramic. The volume of the outer cylinder is calculated according to the gas retention time of 1 s-5 s; the gas inlet is arranged along the circumferential direction of the outer barrel, and the sewage draining outlet is positioned under the bottom of the outer barrel.
Furthermore, the thermal desorption reactor is composed of an outer cylinder, a spiral propeller arranged in the outer cylinder and a heating jacket arranged on the outer wall of the outer cylinder, wherein scraping blades are arranged on spiral blades of the spiral propeller, the scraping blades are arranged in the length range of 1/3-4/5 of continuous spiral blades, and one scraping blade is arranged at intervals of 1/4 screw pitches. The scraping pieces are axially arranged along the spiral rotating shaft, so that the scraping pieces have a scraping effect towards the rotating direction when the rotating shaft rotates, high-calorific-value waste enters the thermal desorption reactor and then becomes a thin-layer state on the inner wall of the outer cylinder, the organic matter desorption efficiency is improved, and coking is avoided when the high-calorific-value dangerous waste is thermally desorbed. The screw pitch of the spiral propeller is preferably 50-550 mm, the distance between the scraping blade and the inner wall of the outer cylinder is preferably 3-15 mm, and the heating jacket is internally provided with a baffle plate for increasing the turbulence degree of smoke and improving the heat efficiency.
Furthermore, the air flotation machine (air flotation machine) can be selected from dissolved air flotation or cavitation air flotation, an oil scraper used for separating dirty oil on the middle surface layer of the air flotation machine from the air flotation machine is arranged at the upper part of the air flotation machine, and a mud scraper used for separating sludge deposited on the bottom part of the air flotation machine from the air flotation machine is arranged at the lower part of the air flotation machine.
Further, dirty oil pump is set up on the dirty oil outlet pipeline of air flotation cell and dirty oil is retrieved, and mud is carried to the storage yard and dries to set up the sludge pump on the mud outlet pipeline to send into the desorption once more and carry out the retreatment, until waste discharge reaches the industry standard, be provided with the water pump on the water purification water outlet pipeline and be used for carrying the air cooler with water.
Furthermore, the stirrer consists of a feed hopper, a stirring tank body, a double-helix stirring paddle and a motor; the feeder hopper sets up at agitator tank body top with the feeding, agitator tank body bottom be provided with the discharge gate of screw conveyer intercommunication, two helical mixing oar sets up in the jar internally, by the pivot with around two helical blade of pivot spiral setting constitute, and two helical blade's helical direction is opposite, and helical blade is provided with the section along the pivot direction, and the sliced cutting edge orientation is the same with the pivot direction.
The above technical scheme of the utility model, the quench tower sprays examination quench tower for current, dry-type quench tower is the same with spraying examination quench tower structure, adopts alkali lye to replace water to spray according to the technology needs in process flow.
Further, the deacidification tower adopts a ceramic corrugated structured packing tower or a bubble tower.
Further, the deionized water air cooler comprises an upper box body, a heat exchange tube group, a lower box body, a water seal pipe and a fan. The heat exchange tube group is welded in the box body, the lower box body is provided with a forced air exhaust fan, and the water seal pipe is connected with the heat exchange tube group to prevent the pressure in the heat exchange tube group from exceeding the limit value born by the system and protect the safe operation of equipment. The forced air flow generated when the fan operates exchanges heat with the deionized water in the heat exchange tube set, and in order to improve the heat exchange efficiency, the heat exchange tube set adopts fins, so that the heat exchange area is increased.
Among the processing system, activated carbon sprayer, air cooler all can be in market purchase. The plasma pyrolysis furnace and the gas combustion reactor can be customized in the market according to the treatment capacity of the system for treating high-calorific-value wastes, and temperature detection related instruments are correspondingly installed on equipment needing to control reaction temperature. The plasma pyrolysis furnace and the plasma torch adopted by the gas combustion reactor are the plasma generator of the patent application with the publication number of CN110248459A proposed by the applicant.
The utility model provides a method for dangerous waste of high calorific value of plasma processing based on above-mentioned processing system, including following step:
the utility model provides a method for high calorific value hazardous waste is handled to plasma uses above-mentioned processing system, includes following content:
starting a plasma pyrolysis unit, preheating the thermal desorption reactor by utilizing plasma high-temperature gas generated by a nitrogen plasma torch in the plasma pyrolysis furnace, starting a conveying unit after the temperature in a heating jacket reaches 300 ℃, and adding high-heat-value dangerous waste into a stirrer; starting a thermal desorption unit, a dioxin removal unit and a plasma desulfurization and denitration unit in sequence, controlling the rotating speed of a thermal desorption reactor to be 1 r/min-45 r/min, the material residence time to be 10-30 min and the material temperature to be 200-450 ℃; controlling the reaction temperature in the plasma pyrolysis furnace to be 450-1100 ℃ and the gas residence time to be 0.5-2 s; the reaction temperature of the gas combustion reactor is controlled to be 1000-1200 ℃, and the gas retention time is 2-5 s.
Further, the high calorific value hazardous waste includes dye waste, leather waste, chemical intermediates, distillation residues, and waste paint residues.
The system processing and processing method has the following working procedures and principles:
the dangerous waste with high calorific value can be mixed into household garbage, such as gloves, iron wires, wood materials and the like, and the substances are prevented from winding and blocking in the screw conveyor and need to be crushed and uniformly mixed. The high-heat value dangerous waste enters a stirring homogenizer, is cut into small pieces under the action of the shearing force of the slices on a rotating shaft of the stirring homogenizer, and is uniformly mixed in the cutting process. The high-heat-value dangerous waste which is cut into a certain size by the stirrer and is uniformly mixed is conveyed to the airlock through the screw conveyor, the airlock is divided into 6-10 small spaces, air in feeding is sealed by the partition plates in each space during operation, and the airlock is connected with a nitrogen outlet of the nitrogen making machine, so that thermal desorption in the thermal desorption reactor is carried out in inert gas components, and primary desorption is carried out.
The heat source of the thermal desorption reactor is derived from flue gas generated by oxygen-enriched combustion of desorption gas generated by a desorption unit and pyrolysis gas generated by a plasma pyrolysis unit in a gas combustion reactor by adopting an oxygen plasma torch, the flue gas flows through a jacket of the thermal desorption reactor to indirectly heat dangerous wastes with high heat values in the thermal desorption reactor, the temperature of materials in the thermal desorption reactor is 200-450 ℃, and the temperature of a flue gas outlet of the thermal desorption reactor is lower than 600 ℃. The high-calorific-value dangerous waste in the reaction cavity inside the thermal desorption reactor is pyrolyzed under the anoxic reaction condition, S and Cl elements in the pyrolysis flue gas of the high-calorific-value dangerous waste exist in the form of hydride, the combustible gas of pyrolysis products mainly comprises hydrogen and carbon monoxide, the rest hydrocarbon is converted into oil, and the pyrolysis flue gas is in a reducing atmosphere, so that NO NO existsXAs a result, the ash mainly contains un-cracked organic matters and a large amount of carbon element solid phase. And outputting the high-temperature solid phase into a water quenching tank, performing water quenching to form glass slag, and fishing the glass slag into a slag dragging machine to be sent to a storage yard for resource recycling.
Gas containing hydrocarbon generated from the thermal desorption reactor enters a quenching tower, water is atomized in the quenching tower through a nozzle and then is in large-area liquid-gas contact with the gas containing the hydrocarbon, the gas containing more than C3 in the hydrocarbon is quenched and cooled by water to form an oil-water mixture, and the gas containing less than C3 and hydrogen directly enter a dioxin removal unit for combustion. The oil-water mixture enters an air flotation machine, the air flotation machine adopts nitrogen as a dissolved air source, the nitrogen generates a large amount of micro bubbles in water through a dissolved air and release system of the air flotation machine, oil drops dispersed in oil water are gathered on the bubbles to cause that the integral density is less than that of the water, the oil rises to the water surface by means of buoyancy, an oil layer is scraped to an oil chamber of the air flotation machine under the action of an oil scraper, and recovered oil is recovered by a sump oil pump after the liquid level in the oil chamber reaches a certain liquid level; when the suspended solid at the bottom of the water chamber in the air flotation machine reaches a certain concentration, the suspended solid is conveyed to a storage yard by a sludge pump to be dried and then conveyed to thermal desorption for secondary treatment. And conveying the water subjected to oil-water separation by the air flotation machine to an air cooler through a circulating water pump for cooling, and then taking the cooled water as cooling water of the quenching tower. Residual ash of the thermal desorption unit directly enters the plasma pyrolysis unit for deep pyrolysis; flue gas of the thermal desorption reactor jacket after heat exchange enters a dry quenching tower of the plasma desulfurization and denitration unit.
The atmosphere in the plasma pyrolysis furnace is inert reducing atmosphere, the autocatalysis effect of high enthalpy, high energy and high activity particles (high energy electrons and unpaired ions) of plasma is utilized to accelerate the pyrolysis reaction of residual organic matters in the high calorific value dangerous waste, and the organic matters are converted into the simplest elemental gases of hydrogen, carbon monoxide and methane under the action of the activity particles generated by the plasma. The temperature of the plasma pyrolysis furnace is controlled to be 450-1100 ℃, the gas retention time is 0.5-2 s, the residue after reaction mainly contains carbon elements and heavy metals, and the heavy metals have lower leachability at high temperature.
In the dioxin removing unit, the reaction temperature of the gas combustion reactor is 1000-1200 ℃, and the gas retention time is 2-5 s. Gasified gas from pyrolysis of the plasma pyrolysis furnace and desorbed gas from the thermal desorption reactor are in direct contact with oxygen plasma jet flow under the high temperature, high enthalpy and high oxidation activity of oxygen plasma, the gasified gas and the desorbed gas are fully reacted with active oxygen active particles with high enthalpy under the turbulent stirring action of the jet flow plasma, single gasified gas and desorbed gas are all converted into carbon dioxide, a precursor of dioxin (without benzene ring) is avoided, and Cl element of dangerous waste with high heat value is desorbed in a desorption unit, so that no dioxin is generated in the unit. Flue gas generated by combustion enters a heating jacket of the thermal desorption reactor to be used as a heat source of the thermal desorption reactor.
Residual acid gas in the flue gas from the thermal desorption reactor is removed through a dry quenching tower under the atomization and spraying effects of alkali liquor, so that a discharge electrode of the low-temperature plasma reactor is protected from being corroded, and the service life of the low-temperature plasma reactor is prolonged. The sprayed alkali liquor is directly contacted with the acid gas to reduce the temperature of the flue gas to 150-200 ℃. The activated carbon ejector directly injects activated carbon powder into a pipeline entering a dry quenching tower and a bag-type dust collector, and the activated carbon absorbs heavy metals with low boiling point and dioxin which is not reacted in a dioxin removal unit. The activated carbon powder for absorbing heavy metal and dioxin and salt powder reacted by the dry type quenching tower are intercepted by the bag-type dust remover to form fly ash which is discharged when a certain amount of fly ash is formed. And (3) introducing the gas filtered by the bag-type dust collector into a low-temperature plasma reactor, and removing nitrogen oxides and sulfides under the auxiliary action of an alcohol solution. The alcohol liquid stored in the alcohol liquid storage tank is conveyed into the low-temperature plasma reactor through the alcohol pump, and during the cathode discharge process of the low-temperature plasma reactor, ∙ CH is generated by the alcohol3、 CH2OH∙、∙CH3O、∙CH2、CH3OH ∙, CH ∙, OH ∙, the hydrocarbons produced in the process also produce free radicals which are formed by the consumption of O2Or O ∙ free radical accelerates the elimination of NO, and can oxidize NO and CO into N2、NO2And CO2OH ∙ generated by alcohol discharge will react with SO2Reaction to OHSO2And HSO3. The flue gas desulfurized and denitrified by the low-temperature plasma reactor enters a deacidification tower, and NO is generated under the action of alkali liquor and the like2、OHSO2And HSO3And neutralizing to generate nitrate and sulfate, and discharging the flue gas with the pollutants removed to a chimney under the suction action of a flue gas exhaust fan.
Compared with the prior art, the utility model discloses following beneficial effect has:
1. the utility model discloses among the process systems, thermal desorption and plasma pyrolysis furnace all adopt inert gas, have avoided high calorific value hazardous waste to reduce the handling capacity of system because of the calorific value is high, and the heavy metal in the lime-ash after handling leaches the toxicity and is less than GB5085.3-2007 hazardous waste and leaches the limit value that leaches toxicity discrimination standard.
2. The utility model discloses process system is through setting up thermal desorption and plasma pyrolysis oven, adopts the segmentation schizolysis to the component characteristic difference of high calorific value hazardous waste, has improved pyrolytic reaction efficiency.
3. The utility model discloses the flue gas that process systems thermal desorption reactor adopted gas combustion reactor oxygen boosting burning to produce has utilized the heat source as the heat source, the energy has been practiced thrift to the high efficiency.
4. The utility model discloses plasma torch of plasma pyrolysis oven adopts nitrogen gas as working medium gas in the process systems, the gaseous gas of plasma pyrolysis oven pyrolysis and the desorption gas that comes from thermal desorption reactor are at the high temperature of oxygen plasma, under high enthalpy and high oxidation activity, with oxygen plasma efflux direct contact, under the torrent stirring effect of jet plasma, carry out abundant reaction with the active oxygen active particle that has of high enthalpy and all turn into carbon dioxide, the production of the predecessor of dioxin (no benzene ring exists) has been avoided, and the Cl element in the dangerous waste material of high calorific value has been deviate from at the desorption unit, consequently, no dioxin generates, reduce the influence to the environment.
5. The utility model discloses process system adopts low temperature plasma to cooperate alcohols absorbent to carry out SOx/NOx control, utilizes low temperature plasma purification technique to improve SOx/NOx control efficiency to required equipment is small, has saved the occupation of land.
6. The utility model discloses the water after air flotation machine separation is used as the cooling water of quench tower after the air cooler cooling in process systems, has practiced thrift the water resource.
Drawings
Fig. 1 is a schematic diagram of the process route layout of the treatment system of the present invention.
Wherein: 1-a stirrer; 2-a screw conveyor; 3-air locking; 4-thermal desorption reactor; 5-a plasma pyrolysis furnace; 6-a gas combustion reactor; 7-a dry quench tower; 8-an activated carbon injector; 9-bag dust collector; a 10-alcohol storage tank; an 11-alcohol pump; 12-a low temperature plasma reactor; 13-low temperature plasma power supply; 14-a deacidification tower; 15-alkali liquor delivery pump; 16-an alkali liquor preparation box; 17-a chimney; 18-a smoke exhaust fan; 19-an alkali liquor circulating pump; 20-a salt storage tank; 21-deionized water air cooler; 22-a humidifying conveyor; 23-a plasma power supply; 24-a quench tower; 25-air cooler; 26-a circulating water pump; 27-an air flotation machine; 28-sludge pump; 29-sump oil pump; 30-nitrogen plasma torch; 31-oxygen plasma torch, 32-nitrogen making machine and 33-deionized water circulating pump.
Detailed Description
The system and the method for treating dangerous waste with high calorific value based on plasma treatment of the present invention are further described in the following embodiments. It should be noted that the following examples are only for illustrating the present invention and should not be construed as limiting the scope of the present invention, and those skilled in the art can make some non-essential improvements and modifications to the present invention according to the above-mentioned contents of the invention and still fall into the scope of the invention.
In the following examples, the activated carbon injector, air cooler, air flotation machine, pump, nitrogen making machine, and plasma power source are all commercially available. The treatment capacity of the plasma pyrolysis furnace, the gas combustion reactor, the low-temperature plasma reactor, the thermal desorption reactor, the stirrer, the deionized water air cooler, the deacidification tower, the quench tower and the like for treating high-calorific-value wastes according to the system is customized in the market, and a temperature detection related instrument is correspondingly installed on equipment needing to control the reaction temperature.
The plasma torch uses the plasma generator described in the applicant's published patent application CN 110248459A.
Example 1
The high-calorific-value dangerous waste treatment system based on plasma treatment comprises a conveying unit, a desorption unit, a plasma pyrolysis unit, a dioxin removal unit, a plasma desulfurization and denitrification unit and an ash output unit;
the conveying unit comprises a stirrer 1, a spiral conveyor 2 communicated with a discharge hole of the stirrer, and an air lock 3 communicated with a discharge hole of the spiral conveyor;
the desorption unit comprises a thermal desorption reactor 4, a spray type quench tower 24, a dissolved air floatation machine 27 for oil-water separation and an air cooler 25; the thermal desorption reactor is provided with a heating jacket, a feed inlet of the thermal desorption reactor is communicated with an airlock discharge port in the conveying unit, a desorption gas outlet of the thermal desorption reactor is communicated with an inlet of a quench tower, a cooled liquid phase outlet of the quench tower is communicated with an inlet of an air floatation machine, a purified water outlet after oil-water separation treatment of the air floatation machine is communicated with an inlet of an air cooler 25, an oil scraper for separating dirty oil on the middle surface layer of the air floatation machine from the air floatation machine is arranged at the upper part of the air floatation machine, and a mud scraper for separating sludge deposited at the bottom of the air floatation machine from the air floatation machine is arranged at the lower part of the air floatation machine; a dirty oil pump 29 is arranged on a dirty oil outlet pipeline of the air flotation machine to recover dirty oil, and a sludge pump 28 is arranged on a sludge outlet pipeline to convey sludge to a storage yard for airing so as to convey the sludge to desorption for secondary treatment again until waste discharge reaches an industrial standard; and a cold water outlet of the air cooler is communicated with a cooling water inlet of the quenching tower, and a purified water outlet pipeline of the air floatation machine is provided with a water pump 26 for conveying water to the air cooler.
The thermal desorption reactor consists of an outer cylinder, a spiral propeller arranged in the outer cylinder and a heating jacket arranged on the outer wall of the outer cylinder, wherein scraping blades are arranged on spiral blades of the spiral propeller, the scraping blades are arranged in the 4/5 length range of continuous spiral blades, and one scraping blade is arranged at intervals of 1/4 screw pitches. The scraping pieces are axially arranged along the spiral rotating shaft, so that the scraping pieces have a scraping effect towards the rotating direction when the rotating shaft rotates, high-calorific-value waste enters the thermal desorption reactor and then becomes a thin-layer state on the inner wall of the outer cylinder, the organic matter desorption efficiency is improved, and coking is avoided when the high-calorific-value dangerous waste is thermally desorbed. The screw pitch of the screw propeller is 50-550 mm, the distance between the scraping blade and the inner wall of the outer cylinder is 15mm, and the heating jacket is internally provided with a baffle plate for increasing the turbulence degree of smoke and improving the heat efficiency.
The stirrer 1 consists of a feed hopper, a stirring tank body, a double-helix stirring paddle and a motor; the feeder hopper sets up at agitator tank body top with the feeding, agitator tank body bottom be provided with the discharge gate of screw conveyer intercommunication, two helical mixing oar sets up in the jar internally, by the pivot with around two helical blade of pivot spiral setting constitute, and two helical blade's helical direction is opposite, and helical blade is provided with the section along the pivot direction, and the sliced cutting edge orientation is the same with the pivot direction.
The plasma pyrolysis unit comprises a plasma pyrolysis furnace 5, a plasma power supply 23, a deionized water air cooler 21 and a nitrogen making machine 32; the plasma pyrolysis furnace consists of a furnace body and a nitrogen plasma torch 30 which is arranged on the furnace body and is used as a heating heat source, a nitrogen outlet of the nitrogen making machine is connected with the nitrogen plasma torch 30 to provide working medium nitrogen for the nitrogen plasma torch, meanwhile, the nitrogen making machine is communicated with an air flotation machine 27 in a desorption unit to provide a dissolved air source for the air flotation machine and is communicated with an air lock 3 in the desorption unit, a plasma power supply 23 is connected with the nitrogen plasma torch to provide a power supply for the plasma torch, and a deionized water air cooler is communicated with a water cooling channel arranged on the nitrogen plasma torch to form a circulating water cooling loop so as to cool nitrogen plasma in work; a feed inlet of the plasma pyrolysis furnace is communicated with a desorption solid phase outlet of a thermal desorption reactor 4 in a desorption unit;
the deionized water air cooler consists of an upper box body, a heat exchange tube group, a lower box body, a water seal pipe and a fan. The heat exchange tube group is welded in the box body, the lower box body is provided with a forced air exhaust fan, and the water seal pipe is connected with the heat exchange tube group to prevent the pressure in the heat exchange tube group from exceeding the limit value born by the system and protect the safe operation of equipment. The forced air flow generated when the fan operates exchanges heat with the deionized water in the heat exchange tube set, and in order to improve the heat exchange efficiency, the heat exchange tube set adopts fins, so that the heat exchange area is increased.
The dioxin extracting unit comprises a plasma gas combustion reactor 6, a plasma power supply 23, a deionized water air cooler 21 and a nitrogen making machine 32, wherein the plasma gas combustion reactor consists of a reaction tank body and an oxygen plasma torch 31 arranged at the top of the tank body, an oxygen outlet of the nitrogen making machine 32 is communicated with the oxygen plasma torch 31 to provide working medium oxygen for the oxygen plasma torch, the plasma power supply 23 is communicated with the oxygen plasma torch to provide a power supply for the oxygen plasma torch, and the deionized water air cooler is communicated with a water cooling channel arranged on the oxygen plasma torch to form a circulating water cooling loop so as to cool the oxygen plasma in working; the gas inlet of the plasma gas combustion reactor 6 is communicated with a gas outlet at the top of the quench tower 24 in the thermal desorption unit and is simultaneously communicated with a pyrolysis gas outlet of the plasma pyrolysis furnace 5, and a flue gas outlet after the combustion reaction of the plasma gas combustion reactor 6 is communicated with an inlet of a heating jacket of the thermal desorption reactor 4 in the thermal desorption unit to provide a thermal desorption reaction heat source.
The plasma pyrolysis furnace and the electric arc plasma torch of the gas combustion reactor adopt a turbulent plasma torch, and the rated power of the turbulent plasma torch is 20 KW.
The plasma desulfurization and denitrification unit comprises a dry quenching tower 7, a bag-type dust collector 9, a low-temperature plasma reactor 12, a low-temperature plasma power supply 13, a ceramic corrugated structured packing deacidification tower 14, an alkali liquor preparation box 16 for preparing an alkali liquor sodium hydroxide solution, a salt storage box 20 and an alcohol storage box (10); the dry quenching tower 7 has the same structure as the spraying test quenching tower, cooling water is replaced by alkali liquor, an air inlet of the dry quenching tower 7 is communicated with an outlet of a heating jacket of the thermal desorption reactor 4, an outlet of the dry quenching tower is communicated with an inlet of a bag-type dust remover, an outlet of the bag-type dust remover 9 is communicated with an inlet of a low-temperature plasma reactor 12, an activated carbon injector 8 for injecting activated carbon into a communicating pipeline is arranged on the communicating pipeline, an outlet of the low-temperature plasma reactor 12 is communicated with an air inlet of an deacidification tower 14, and a gas outlet of the deacidification tower is communicated with the atmosphere; alkali liquor inlets for denitration and desulfurization are formed in the dry-type quenching tower 7 and the deacidification tower 14; an alkali liquor outlet of the alkali liquor preparation box is respectively communicated with alkali liquor inlets of the dry quenching tower 7 and the deacidification tower 14 through an alkali liquor delivery pump 15, and the alkali liquor is delivered to the dry quenching tower and the deacidification tower to remove residual acid gas in the flue gas. The liquid phase outlet of the deacidification tower 14 is communicated with a salt storage tank to collect the salt obtained after desulfurization and denitrification and surplus alkali liquor, and the outlet of the salt storage tank is communicated with an alkali liquor preparation tank through an alkali liquor circulating pump 19 to realize the recycling of the alkali liquor. The alcohol storage tank is communicated with a low-temperature plasma reactor 12 through an alcohol pump 11 to provide alcohol solution required by reaction. And a smoke exhaust fan 18 and a chimney 17 are sequentially arranged at a gas outlet of the deacidification tower 14, so that the desulfurized and denitrated flue gas is smoothly discharged.
The low-temperature plasma reactor is based on a double-action mechanism of corona discharge and dielectric barrier discharge, a plurality of discharge tips are concentrically arranged at the anode of the reactor in an outer cylinder container, an electric field with extremely high strength can be generated after voltage is applied to the anode, so that corona discharge occurs, gas enters the reactor container and contacts with the discharge tips, nitrogen oxide and sulfide in the gas are rapidly decomposed in a corona area under the action of alcohol substances, the nitrogen oxide is converted into nitrogen, sulfur dioxide is converted into OHSO2And HSO3. The low-temperature plasma reactor structure comprises an electrode serving as a positive electrode and an outer cylinder serving as a negative electrode; the outer cylinder body is provided with a gas inlet, a gas outlet and a sewage outlet; the electrode (anode) is uniformly arranged on the wall surface of the outer cylinder along the circumferential direction of the outer cylinder, the part of the electrode positioned in the outer cylinder is a conical electrode tip (the major diameter of a cone is 5-20 mm, the minor diameter tip is 1-2 mm, the length of a cone part is 20-100 mm), the distance between adjacent cones is 10-50 mm, the tips of the adjacent electrodes are staggered on the radial plane of the outer cylinder, and the staggered angle is 30-90 degrees; the electrode and the outer cylinder are separated by an insulating material, the thickness of the insulating material is more than 20mm, and the insulating material can be high-density polyethylene or PEK or ceramic. The volume of the outer cylinder is calculated according to the gas retention time of 1s, and the rated power is 15 KW. The distance between the conical tip of the anode and the bottom of the outer cylinder is 20-100 mm; the length of the part of the positive electrode outside the outer cylinder body meets the wiring requirement. The gas inlet is arranged along the circumferential direction of the outer cylinder body in a tangential manner, and the central line of the gas inlet is positioned at a position which is 200-400 mm away from the bottom of the outer cylinder body; the drain outlet is positioned under the bottom of the outer barrel. The central line of the gas outlet is positioned at 250-550 mm of the top of the outer cylinder.
The ash output unit comprises a water quenching box and a slag conveyor 22, and molten liquid pyrolyzed in the plasma pyrolysis furnace of the plasma pyrolysis unit is quenched and then is salvaged and recovered by the slag conveyor.
Example 2
A method of plasma treating high calorific value hazardous waste printing and dyeing waste (provided with cullet and calcium oxide) based on the treatment system described in example 1 comprising the steps of:
the treatment amount of the printing and dyeing waste is 6 Kg/h. Starting a plasma pyrolysis unit, preheating the thermal desorption reactor by utilizing plasma high-temperature gas generated by a nitrogen plasma torch in the plasma pyrolysis furnace, starting a conveying unit after the temperature in a heating jacket reaches 300 ℃, and adding high-heat-value dangerous waste into a stirrer; sequentially starting a thermal desorption unit, a dioxin desorption unit and a plasma desulfurization and denitration unit, and controlling the rotating speed of a thermal desorption reactor to be 1 r/min-45 r/min and the material temperature to be 300 ℃; controlling the reaction temperature in the plasma pyrolysis furnace to be 1000 ℃; the reaction temperature of the gas combustion reactor was controlled to 1200 ℃.
The workflow and principle are as follows:
the dangerous waste with high calorific value can be mixed into household garbage, such as gloves, iron wires, wood materials and the like, and the substances are prevented from winding and blocking in the screw conveyor and need to be crushed and uniformly mixed. The high-heat value dangerous waste enters a stirring homogenizer, is cut into small pieces under the action of the shearing force of the slices on a rotating shaft of the stirring homogenizer, and is uniformly mixed in the cutting process. The high-heat-value dangerous waste which is cut into a certain size by the stirrer and is uniformly mixed is conveyed to the airlock through the screw conveyor, the airlock is divided into 6-10 small spaces, air in feeding is sealed by the partition plates in each space during operation, and the airlock is connected with a nitrogen outlet of the nitrogen making machine, so that thermal desorption in the thermal desorption reactor is carried out in inert gas components, and primary desorption is carried out.
The heat source of the thermal desorption reactor is flue gas generated by oxygen-enriched combustion of desorption gas generated by a desorption unit and pyrolysis gas generated by a plasma pyrolysis unit in a gas combustion reactor by adopting an oxygen plasma torch, and the high-heat value hazardous waste in the thermal desorption reactor is treated by the flue gas flowing through a jacket of the thermal desorption reactorIndirect heating, wherein the temperature of the materials in the thermal desorption reactor is 300 ℃, and the temperature of the flue gas outlet of the thermal desorption reactor is lower than 600 ℃. The high-calorific-value dangerous waste in the reaction cavity inside the thermal desorption reactor is pyrolyzed under the anoxic reaction condition, S and Cl elements in the pyrolysis flue gas of the high-calorific-value dangerous waste exist in the form of hydride, the combustible gas of pyrolysis products mainly comprises hydrogen and carbon monoxide, the rest hydrocarbon is converted into oil, and the pyrolysis flue gas is in a reducing atmosphere, so that NO NO existsXAs a result, the ash mainly contains un-cracked organic matters and a large amount of carbon element solid phase. And outputting the high-temperature solid phase into a water quenching tank, performing water quenching to form glass slag, and fishing the glass slag into a slag dragging machine to be sent to a storage yard for resource recycling.
Gas containing hydrocarbon generated from the thermal desorption reactor enters a quenching tower, water is atomized in the quenching tower through a nozzle and then is in large-area liquid-gas contact with the gas containing the hydrocarbon, the gas containing more than C3 in the hydrocarbon is quenched and cooled by water to form an oil-water mixture, and the gas containing less than C3 and hydrogen directly enter a dioxin removal unit for combustion. The oil-water mixture enters an air flotation machine, the air flotation machine adopts nitrogen as a dissolved air source, the nitrogen generates a large amount of micro bubbles in water through a dissolved air and release system of the air flotation machine, oil drops dispersed in oil water are gathered on the bubbles to cause that the integral density is less than that of the water, the oil rises to the water surface by means of buoyancy, an oil layer is scraped to an oil chamber of the air flotation machine under the action of an oil scraper, and recovered oil is recovered by a sump oil pump after the liquid level in the oil chamber reaches a certain liquid level; when the suspended solid at the bottom of the water chamber in the air flotation machine reaches a certain concentration, the suspended solid is conveyed to a storage yard by a sludge pump to be dried and then conveyed to thermal desorption for secondary treatment. And conveying the water subjected to oil-water separation by the air flotation machine to an air cooler through a circulating water pump for cooling, and then taking the cooled water as cooling water of the quenching tower. Residual ash of the thermal desorption unit directly enters the plasma pyrolysis unit for deep pyrolysis; flue gas of the thermal desorption reactor jacket after heat exchange enters a dry quenching tower of the plasma desulfurization and denitration unit.
The atmosphere in the plasma pyrolysis furnace is inert reducing atmosphere, the autocatalysis effect of high enthalpy, high energy and high activity particles (high energy electrons and unpaired ions) of plasma is utilized to accelerate the pyrolysis reaction of residual organic matters in the high calorific value dangerous waste, and the organic matters are converted into the simplest elemental gases of hydrogen, carbon monoxide and methane under the action of the activity particles generated by the plasma. The temperature of the plasma pyrolysis furnace is controlled to be 1000 ℃, the residue after reaction mainly contains carbon element and heavy metal, and the heavy metal has lower leachability at high temperature.
In the dioxin removal unit, the reaction temperature of the gas combustion reactor is 1200 ℃. Gasified gas from pyrolysis of the plasma pyrolysis furnace and desorbed gas from the thermal desorption reactor are in direct contact with oxygen plasma jet flow under the high temperature, high enthalpy and high oxidation activity of oxygen plasma, the gasified gas and the desorbed gas are fully reacted with active oxygen active particles with high enthalpy under the turbulent stirring action of the jet flow plasma, single gasified gas and desorbed gas are all converted into carbon dioxide, a precursor of dioxin (without benzene ring) is avoided, and Cl element of dangerous waste with high heat value is desorbed in a desorption unit, so that no dioxin is generated in the unit. Flue gas generated by combustion enters a heating jacket of the thermal desorption reactor to be used as a heat source of the thermal desorption reactor.
Residual acid gas in the flue gas from the thermal desorption reactor is removed through a dry quenching tower under the atomization and spraying effects of alkali liquor, so that a discharge electrode of the low-temperature plasma reactor is protected from being corroded, and the service life of the low-temperature plasma reactor is prolonged. The sprayed alkali liquor is directly contacted with the acid gas to reduce the temperature of the flue gas to 150-200 ℃. The activated carbon ejector directly injects activated carbon powder into a pipeline entering a dry quenching tower and a bag-type dust collector, and the activated carbon absorbs heavy metals with low boiling point and dioxin which is not reacted in a dioxin removal unit. The activated carbon powder for absorbing heavy metal and dioxin and salt powder reacted by the dry type quenching tower are intercepted by the bag-type dust remover to form fly ash which is discharged when a certain amount of fly ash is formed. And (3) introducing the gas filtered by the bag-type dust collector into a low-temperature plasma reactor, and removing nitrogen oxides and sulfides under the auxiliary action of an alcohol solution. The alcohol liquid stored in the alcohol liquid storage tank is conveyed to the low-temperature plasma reactor through the alcohol pumpIn the process of discharging the cathode of the low-temperature plasma reactor, ∙ CH is generated from alcohol3、 CH2OH∙、∙CH3O、∙CH2、CH3OH ∙, CH ∙, OH ∙, the hydrocarbons produced in the process also produce free radicals which are formed by the consumption of O2Or O ∙ free radical accelerates the elimination of NO, and can oxidize NO and CO into N2、NO2And CO2OH ∙ generated by alcohol discharge will react with SO2Reaction to OHSO2And HSO3. The flue gas desulfurized and denitrified by the low-temperature plasma reactor enters a deacidification tower, and NO is generated under the action of alkali liquor and the like2、OHSO2And HSO3And neutralizing to generate nitrate and sulfate, and discharging the flue gas with the pollutants removed to a chimney under the suction action of a flue gas exhaust fan.
After treatment, the volume reduction rate reached 96.3%, and the ash and gas detection results are shown in the table below.
Table 1.
Note: ND-not detected
Table 2.
Note: ND-was not detected.
Example 3
The paint residue waste (with cullet and calcium oxide) was treated using the treatment system described in example 1 at a throughput of 6Kg/h, comprising the following steps:
starting a plasma pyrolysis unit, preheating the thermal desorption reactor by utilizing plasma high-temperature gas generated by a nitrogen plasma torch in the plasma pyrolysis furnace, starting a conveying unit after the temperature in a heating jacket reaches 300 ℃, and adding high-heat-value dangerous waste into a stirrer; starting the thermal desorption unit, the dioxin desorption unit and the plasma desulfurization and denitration unit in sequence, and controlling the rotating speed of the thermal desorption reactor to be 1 r/min-45 r/min and the material temperature to be 450 ℃; controlling the reaction temperature in the plasma pyrolysis furnace to be 1050 ℃; the reaction temperature of the gas combustion reactor was controlled to 1200 ℃. The low temperature plasma reactor employs the structure described herein with a gas residence time of 2s therein.
The volume reduction rate after treatment reaches 95.6 percent, and the detection results of ash and gas are shown in the following table.
Table 3.
Note: ND-was not detected.
Table 4.
Note: ND-was not detected.
Claims (9)
1. A high-calorific-value dangerous waste treatment system based on plasma treatment is characterized by comprising a conveying unit, a desorption unit, a plasma pyrolysis unit, a dioxin desorption unit, a plasma desulfurization and denitrification unit and an ash output unit;
the conveying unit comprises a stirrer (1), a spiral conveyor (2) communicated with a discharge hole of the stirrer, and an air lock (3) communicated with a discharge hole of the spiral conveyor;
the desorption unit comprises a thermal desorption reactor (4), a quench tower (24), an air flotation machine (27) for oil-water separation and an air cooler (25); the thermal desorption reactor is provided with a heating jacket, a feed inlet of the thermal desorption reactor is communicated with an airlock discharge port in the conveying unit, a desorption gas outlet of the thermal desorption reactor is communicated with an inlet of a quench tower, a cooled liquid phase outlet of the quench tower is communicated with an inlet of an air floatation machine, a purified water outlet after oil-water separation treatment of the air floatation machine is communicated with an inlet of an air cooler (25), and a cold water outlet of the air cooler is communicated with a cooling water inlet of the quench tower;
the plasma pyrolysis unit comprises a plasma pyrolysis furnace (5), a plasma power supply (23), a deionized water air cooler (21) and a nitrogen making machine (32); the plasma pyrolysis furnace consists of a furnace body and a nitrogen plasma torch (30) which is arranged on the furnace body and is used as a heating heat source, a nitrogen outlet of the nitrogen making machine is connected with the nitrogen plasma torch (30) to provide working medium nitrogen for the nitrogen plasma torch, and is communicated with an air flotation machine (27) in a desorption unit to provide a dissolved air source for the air flotation machine and communicated with an air lock (3) in the desorption unit, the plasma power source (23) is connected with the nitrogen plasma torch to provide a power source for the plasma torch, and the deionized water air cooler is communicated with a water cooling channel arranged on the nitrogen plasma torch to form a circulating water cooling loop so as to cool the nitrogen plasma in work; a feed inlet of the plasma pyrolysis furnace is communicated with a desorption solid phase outlet of a thermal desorption reactor (4) in a desorption unit;
the dioxin extracting unit comprises a plasma gas combustion reactor (6), a plasma power supply (23), a deionized water air cooler (21) and a nitrogen making machine (32), wherein the plasma gas combustion reactor consists of a reaction tank body and an oxygen plasma torch (31) installed at the top of the tank body, an oxygen outlet of the nitrogen making machine (32) is communicated with the oxygen plasma torch (31) to provide working medium oxygen for the oxygen plasma torch, the plasma power supply (23) is communicated with the oxygen plasma torch to provide a power supply for the oxygen plasma torch, and the deionized water air cooler is communicated with a water cooling channel arranged on the oxygen plasma torch to form a circulating water cooling loop so as to cool the oxygen plasma in work; an air inlet of the plasma gas combustion reactor (6) is communicated with a gas outlet at the top of a quench tower (24) in the thermal desorption unit and is also communicated with a pyrolysis gas outlet of the plasma pyrolysis furnace (5), a flue gas outlet after combustion reaction of the plasma gas combustion reactor (6) is communicated with an inlet of a heating jacket of a thermal desorption reactor (4) in the thermal desorption unit, and a thermal desorption reaction heat source is provided;
the plasma desulfurization and denitrification unit comprises a dry quenching tower (7), a bag-type dust collector (9), a low-temperature plasma reactor (12), a low-temperature plasma power supply (13) and a deacidification tower (14); an air inlet of the dry quenching tower (7) is communicated with an outlet of a heating jacket of the thermal desorption reactor (4), an outlet of the dry quenching tower is communicated with an inlet of a bag-type dust remover, an outlet of the bag-type dust remover (9) is communicated with an inlet of a low-temperature plasma reactor (12), an activated carbon ejector (8) for ejecting activated carbon into a communicating pipeline is arranged on the communicating pipeline, an outlet of the low-temperature plasma reactor (12) is communicated with an air inlet of an acid removal tower (14), and a gas outlet of the acid removal tower is communicated with the atmosphere; alkali liquor inlets for denitration and desulfurization are formed in the dry quenching tower (7) and the deacidification tower (14);
the ash output unit comprises a water quenching box and a slag conveyor (22), and molten liquid pyrolyzed in the plasma pyrolysis furnace of the plasma pyrolysis unit is quenched and then recovered by the slag conveyor.
2. The treatment system according to claim 1, wherein the plasma desulfurization and denitrification unit is further provided with an alkali liquor preparation box (16) for preparing an alkali liquor sodium hydroxide solution, an alkali liquor outlet of the alkali liquor preparation box is respectively communicated with alkali liquor inlets of the dry quenching tower (7) and the deacidification tower (14) through an alkali liquor conveying pump (15), and the alkali liquor is conveyed to the dry quenching tower and the deacidification tower to remove residual acid gas in the flue gas; the plasma SOx/NOx control unit still is provided with salt storage tank (20), the liquid phase export of deacidification tower (14) and salt storage tank intercommunication to collect gained salt and surplus alkali lye after the SOx/NOx control, the export of salt storage tank is prepared the case through alkali lye circulating pump (19) and alkali lye and is communicated, realizes the cyclic utilization of alkali lye.
3. The treatment system as claimed in claim 1, wherein an oil scraper for separating dirty oil on the surface layer of the air flotation machine from the air flotation machine is arranged at the upper part of the air flotation machine, and a mud scraper for separating sludge deposited at the bottom of the air flotation machine from the air flotation machine is arranged at the lower part of the air flotation machine; dirty oil pump (29) is set up on the dirty oil outlet pipeline of air supporting flotation machine and is retrieved dirty oil, sets up sludge pump (28) on the mud outlet pipeline and carry to the storage yard with mud and dry to send desorption once more and carry out the retreatment, until waste discharge reaches the industry standard, be provided with water pump (26) on the water purification outlet pipeline and be used for carrying the air cooler with water.
4. The treatment system according to claim 1, wherein a smoke exhaust fan (18) and a chimney (17) are sequentially arranged at the gas outlet of the deacidification tower (14) to smoothly discharge the desulfurized and denitrified flue gas.
5. The treatment system according to claim 1, wherein the plasma desulfurization and denitrification unit is further provided with an alcohol storage tank (10) which is communicated with the low-temperature plasma reactor (12) through an alcohol pump (11) and provides alcohol solution required by the reaction.
6. The processing system of claim 1, wherein the low temperature plasma reactor structure comprises an electrode as a positive electrode, an outer cylinder as a negative electrode; the outer cylinder body is provided with a gas inlet, a gas outlet and a sewage outlet; the electrodes are uniformly arranged on the wall surface of the outer cylinder along the circumferential direction of the outer cylinder, the part of the electrode positioned in the outer cylinder is a conical electrode tip along the radial direction of the outer cylinder, the adjacent electrode tips are staggered on the radial plane of the outer cylinder, and the mutual staggered angle is 30-90 degrees; the electrode and the outer cylinder are separated by insulating material; the gas inlet is arranged along the circumferential direction of the outer barrel, and the sewage draining outlet is positioned under the bottom of the outer barrel.
7. The treatment system according to claim 1, wherein the thermal desorption reactor comprises an outer cylinder, a screw propeller arranged in the outer cylinder, and a heating jacket arranged on the outer wall of the outer cylinder, wherein the screw blades of the screw propeller are provided with scraping blades, the scraping blades are arranged in the range of 1/3-4/5 of the continuous screw blades, and one scraping blade is arranged at intervals of 1/4 screw pitches; the scraping blade is arranged along the axial direction of the spiral rotating shaft, so that the scraping blade has a scraping effect towards the rotating direction when the rotating shaft rotates; the heating jacket is internally provided with a baffle plate for increasing the turbulence degree of the flue gas and improving the heat efficiency.
8. The treatment system according to claim 1, wherein the stirrer (1) consists of a feed hopper, a stirring tank body, a double-helix stirring paddle and a motor; the feeder hopper sets up at agitator tank body top with the feeding, agitator tank body bottom be provided with the discharge gate of screw conveyer intercommunication, two helical mixing oar sets up in the jar internally, by the pivot with around two helical blade of pivot spiral setting constitute, and two helical blade's helical direction is opposite, and helical blade is provided with the section along the pivot direction, and the sliced cutting edge orientation is the same with the pivot direction.
9. The treatment system of claim 1, wherein the acid removal column is a ceramic corrugated structured packing column or a bubble column.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112984783A (en) * | 2021-02-05 | 2021-06-18 | 陕西翼飞航智能科技有限公司 | Based on CO2Cement production and CO production in plasma hot blast stove2Decomposed gas recovery system and method |
| CN113617531A (en) * | 2021-08-12 | 2021-11-09 | 杭州灰弘环保科技有限公司 | Flotation removal and degradation method for dioxin in household garbage incineration fly ash |
| RU2809374C1 (en) * | 2023-05-18 | 2023-12-11 | Общество с ограниченной ответственностью "ЭКОЛОГИСТИКА" | Method of plasmothermal processing of solid waste |
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2019
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112984783A (en) * | 2021-02-05 | 2021-06-18 | 陕西翼飞航智能科技有限公司 | Based on CO2Cement production and CO production in plasma hot blast stove2Decomposed gas recovery system and method |
| CN113617531A (en) * | 2021-08-12 | 2021-11-09 | 杭州灰弘环保科技有限公司 | Flotation removal and degradation method for dioxin in household garbage incineration fly ash |
| RU2809374C1 (en) * | 2023-05-18 | 2023-12-11 | Общество с ограниченной ответственностью "ЭКОЛОГИСТИКА" | Method of plasmothermal processing of solid waste |
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