CN216005774U - Marine solid waste plasma gasification melting system - Google Patents
Marine solid waste plasma gasification melting system Download PDFInfo
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- CN216005774U CN216005774U CN202122106101.5U CN202122106101U CN216005774U CN 216005774 U CN216005774 U CN 216005774U CN 202122106101 U CN202122106101 U CN 202122106101U CN 216005774 U CN216005774 U CN 216005774U
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Abstract
The utility model relates to a marine solid waste plasma gasification melting system, which comprises a feeding device, a plasma gasification melting chamber, a gasification combustion chamber and a flue gas heat exchanger, wherein the output end of the feeding device is connected with the feed inlet of the plasma gasification melting chamber; a group of plasma torches are uniformly arranged on the side wall of the plasma gasification melting chamber along the circumferential direction of the side wall, the plasma gasification melting chamber is provided with a synthesis gas circulation reflux device, and flue gas heat exchange is carried outThe preheated air outlet of the dryer is connected with an external heating type drying device arranged outside the feeding device through a preheated air pipeline. The utility model has the advantages that dioxin and NO are effectively inhibitedXThe ash is thoroughly and harmlessly generated, the organic matters are decomposed into combustible synthetic gas, and the combustion performance of combustible gas generated by pyrolysis and gasification is superior to that of the conventional solid waste treatment device on the ship.
Description
Technical Field
The utility model belongs to the technical field of shipbuilding and incineration, a marine solid useless processing system is related to, concretely relates to marine solid useless plasma gasification melting system can handle and wear multiple mixed discarded object.
Background
It is understood that the treatment of the domestic garbage on the ship mainly adopts an incineration mode, and the traditional domestic garbage incineration for the ship has the following problems:
firstly, traditional marine domestic waste burns burning furnace need consume fossil energy such as a large amount of diesel oil and burn supplementarily, for example chinese patent CN2013103098789 provides a marine burning furnace combustion system of two combustion chambers, and wherein the combustion-supporting agent just uses diesel oil in a large number, and fossil fuel's burning can increase the flue gas production volume on the one hand, and on the other hand is under the situation that fossil energy worried about, has aggravated the scarce condition of fossil energy.
Secondly, according to the content display in the MEPC 244-66, the marine incinerator only regulates the temperature of discharged flue gas, the content of CO, the ash discharge amount, unburned components in ash and the like, and does not regulate acid gas, dioxin, heavy metal and the like. At present, high-temperature flue gas in a traditional marine incinerator is directly discharged after being mixed with air and cooled, and flue gas purification is not carried out. The preheated auxiliary fuel oil of the marine incinerator has high sulfur content, and the auxiliary fuel oil, acid gas and dioxin in the solid waste on the ship can generate secondary pollution to the atmosphere.
Thirdly, the combustion temperature of the traditional marine domestic garbage incinerator is 850-1000 ℃, dioxin is not completely decomposed during combustion, the combustion of residual carbon and ash is not complete, and unburned components account for about 10% of the total amount. The combustion performance of solid waste is poor, the air excess coefficient is large and is generally 1.8-2.0, and high-temperature flue gas generated by combustion is directly mixed with 2-5 times of cold air, so that the flue gas emission can be further increased. And the cleanliness and the combustion performance of the combustible gas are superior to those of the direct incineration of the solid waste.
Since the 1990 s, the plasma technology has entered civilian use, and research on the plasma foundation has been gradually started. The temperature of the gasification furnace is increased by introducing thermal plasma arc into the plasma gasification melting, the central temperature of the plasma gasification can reach 6000 ℃, the temperature in the furnace is kept at the same temperature of 1000-1600 ℃, the reaction activity in the furnace is high, and various reactants are completely cracked; the organic matter is converted into synthesis gas, and the inorganic matter is converted into clinker of vitreous body. However, the plasma technology has not been widely popularized and applied to the solid hazardous waste treatment process, and the main reason is that the manufacturing cost and the energy consumption of the plasma torch are high. Meanwhile, due to the special environment of the ship, the ship cannot store gas and cannot treat solid waste by adopting a plasma technology.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem, overcome prior art's shortcoming, a marine solid waste plasma gasification melting system is provided, this system is through combining gasification technique and plasma square, only need the consumption power can solve the fossil fuel problem of burning, the plasma square provides the high temperature oxygen deficiency environment, generate the synthetic gas with the organic matter, the inorganic matter melts into the vitreous body, and the production of acid gas and dioxin can be restrained to the oxygen deficiency, the synthetic gas has good combustion performance, can further reduce the gas emission volume less with pollutant concentration, the energy consumption of the reducible plasma torch of rethread recycle part synthetic gas.
In order to solve the technical problem, the utility model provides a marine solid useless plasma gasification melting system, including feed arrangement, plasma gasification melting chamber, gasification combustion chamber and flue gas heat exchanger, feed arrangement's output links to each other with the feed inlet of plasma gasification melting chamber, the synthetic gas export of plasma gasification melting chamber links to each other with the synthetic gas entry of gasification combustion chamber, the flue gas export of gasification combustion chamber links to each other with the flue gas entry of flue gas heat exchanger; the side wall of the plasma gasification melting chamber is uniformly provided with a group of first plasma torches along the circumferential direction, the plasma gasification melting chamber is provided with a synthesis gas circulating reflux device, a preheated air outlet of the flue gas heat exchanger is connected with an external heating type drying device arranged outside the feeding device through a preheated air pipeline, and energy consumption required by gasification melting of the system is supplemented by releasing heat through combustion of part of combustible gas.
The utility model discloses a system combines together pyrolysis gasification technique and plasma torch's high heat energy, gasifies into combustible synthesis gas earlier on the ship, and the synthesis gas fully burns again, and lime-ash and carbon residue are the melting under plasma torch high temperature effect, provide through synthesis gas backward flow and plasma torch the utility model discloses required energy consumption reduces the consumption of fossil energy such as diesel oil. The pyrolysis gasification needs to be carried out in an oxygen-deficient environment with an air equivalent coefficient of 0-0.3, and the oxygen-deficient environment can effectively inhibit NOXThe plasma torch is used for arc striking under high pressure to release heat energy and provide high temperature of 1100-1600 ℃ for the gasification melting chamber. At the high temperature, organic matters are cracked into combustible synthetic gas, inorganic matters are fused into vitreous bodies, dioxin is completely and instantly decomposed at the high temperature, and the ash burning reduction rate is far less than 10% of the marine standard. The generated synthesis gas has good combustion performance, the air excess coefficient is small and is about 1.2-1.4, and the synthesis gas can be fully combusted in a gasification combustion chamber. The whole energy consumption of the system comes from electric energy, and fossil energy consumption is avoided.
The utility model discloses a marine solid useless processing apparatus is with clean processing as the main objective, retrieves partial synthetic gas and high temperature flue gas waste heat, and its synthetic gas calorific value is up to 6000 ~ 15000KJ/m3Therefore, the energy consumption of the plasma torch system can be reduced by burning the high-calorific-value synthesis gas and utilizing the waste heat of the high-temperature flue gas.
The utility model discloses further optimized technical scheme as follows:
furthermore, the plasma gasification melting chamber is divided into a gasification area and an ash slag melting area, the feeding device and the synthesis gas circulating and refluxing device are arranged in the gasification area, and a slag discharge port is arranged at the bottom of the ash slag melting area.
In the above structure, the synthesis gas passing chamber at the upper part of the plasma gasification melting chamberThe gas-forming circulation reflux device is divided into two parts, one part of the gas-forming circulation reflux device is refluxed to a gasification area of the plasma gasification melting chamber, and CO and H in the gas-forming circulation reflux device2、CH4The heat required by the reaction is released by combustion, so that the power consumption required by pyrolysis and gasification can be reduced, the water vapor in the backflow synthesis gas is used as a gasification agent and is supplemented to a gasification zone, and the pure air gasification agent has no nitrogen introduced into the water vapor, so that the heat value and the purity of the synthesis gas can be improved; and introducing the other part of the synthesis gas into the gasification combustion chamber for secondary complete combustion. The utility model discloses a required energy consumption of system comes from plasma torch electrical heating and the partial combustion heat of synthetic gas, need not to adopt other auxiliary heat sources such as diesel oil, coal, natural gas, has reduced fossil energy resource consumption and the flue gas volume that produces from this.
Furthermore, 2-4 first plasma torches are obliquely arranged at the joint between the ash slag melting zone and the gasification zone, and 2-4 primary air inlets are obliquely arranged on the side wall of the gasification zone.
In the structure, the first plasma torch and the primary air inlet are tangentially arranged, so that the air and the plasma torch are fully mixed to form better cyclone.
Further, the inclined installation angles of the first plasma torch and the primary air inlet are both 35 degrees, the output power of the first plasma torch is 50-500 KW, and the primary air inlet is provided with a first adjusting valve.
Furthermore, the synthesis gas circulation reflux device comprises a synthesis gas reflux pipe, a proportional flow valve is arranged on the synthesis gas reflux pipe, the synthesis gas reflux pipe is connected with a synthesis gas reflux pump, the inlet of the synthesis gas reflux pipe is connected with the upper synthesis gas outlet of the gasification area, and the outlet is connected with the lower synthesis gas inlet of the gasification area.
Thus, part of the synthesis gas in the upper part of the gasification zone flows to the lower part of the gasification zone through the synthesis gas return pipe to carry out oxidation reaction so as to release part of heat required by gasification melting and provide gasifying agent-water. And the residual synthesis gas in the gasification zone enters a gasification combustion chamber through a synthesis gas outlet for incineration. In the pyrolysis gasification reaction, the synthesis gas generated by water-air mixed gasification has high quality and cleanlinessThe synthesis efficiency and the like are better than those of air as a gasifying agent because the air gasifying agent can bring 79 percent of N2The calorific value and cleanliness of the diluted synthesis gas.
Further, feed arrangement includes feed bin, spiral pusher and feeding chute, the sub-unit connection spiral pusher of feed bin, the afterbody of spiral pusher connects the feeding chute, be equipped with external hot type drying device outside the spiral pusher, the pusher adopts external hot mode to carry out the drying to the material, and the temperature of the high temperature flue gas that the heating adopted is about 600 ℃, and the high temperature flue gas comes from gas heat exchanger, 35 ~ 55 contained angles have between feeding chute and the gasification melting chamber.
Furthermore, the external heating type drying device comprises a cylindrical shell, the shell is arranged outside the spiral material pushing device, an inlet of the shell is connected with a preheated air outlet of the flue gas heat exchanger through a preheated air pipeline, an outlet of the shell is connected with the inside of the plasma gasification melting chamber, and the preheated air pipeline is connected with the high-temperature pump.
Further, the top of gasification combustion chamber is equipped with second plasma torch, the output of second plasma torch is 35 ~ 50KW, 2 ~ 4 secondary air entry are installed to the slope on the lateral wall of gasification combustion chamber, secondary air entry is equipped with second adjusting valve, and secondary air entry's slope installation angle is 35, and the lower part of gasification combustion chamber is provided with the synthetic gas entry, and upper portion is provided with the exhanst gas outlet to be located exhanst gas outlet department and be provided with the draught fan on the upper portion of gasification combustion chamber, the mode of going up out under the gasification combustion chamber adoption, high temperature flue gas passes through the draught fan at the top and discharges.
Further, the flue gas heat exchanger comprises a shell and a heat exchange tube arranged in the shell, wherein the shell is provided with a flue gas inlet and a flue gas outlet, and the heat exchange tube is provided with an air inlet and a preheated air outlet.
The utility model discloses a shell and tube gas-gas heat exchanger preheats the air, and the temperature that its flue gas advances, exports is 1200/700, and the temperature that the air advances, exports is normal atmospheric temperature 650, and the high temperature flue gas is discharged in order to avoid the resynthesis of dioxin after the rapid cooling, and the air that is preheated carries out the drying through indirect heat transfer mode to the material again. Therefore, part of high-temperature flue gas heat recovered by the flue gas heat exchanger is used for drying solid waste, and the amount of cold air required by quenching outlet flue gas can be reduced.
The utility model has the advantages that the oxygen deficiency environment of plasma gasification melting chamber has effectively restrained the formation of dioxin and NOX, and the 1100 ~ 1600 ℃ high temperature environment that the plasma torch provided for the dioxin is whole to be decomposed, and the lime-ash is thoroughly innoxious, and the organic matter decomposes into combustible synthesis gas, and the combustion performance of the combustible gas that the pyrolysis gasification generated is superior to on-board traditional solid useless processing apparatus. The utility model discloses a required energy consumption of system is whole to come from the electric energy to through partial synthetic gas backward flow and gas heater's heat exchange, slowed down the energy consumption of plasma torch, solved traditional marine burning furnace that burns need consume a large amount of fossil energy and supplementally burn, aggravation energy consumption lack and fossil burning burn and discharge flue gas scheduling problem. Additionally, the utility model discloses flue gas after the heat transfer of flue gas heat exchanger quenches to 200 ℃, has avoided dioxin resynthesis, has solved the marine solid waste incinerator burning inadequately, and flue gas secondary pollution, lime-ash heat are burnt and are subtracted rate height, the big scheduling problem of flue gas volume to slow down the high energy consumption problem of plasma system.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
In the figure: 1 is a storage bin, 2 is a spiral pusher, 3 is a feeding chute, 4 is a plasma gasification melting chamber, 5 is a primary air inlet, 6 is a first plasma torch, 7 is a synthetic gas conveying pipeline, 8 is a synthetic gas return pipe, 9 is an ash slag melting area, 10 is a gasification area, 11 is a gasification combustion chamber, 12 is a second plasma torch, 13 is a secondary air inlet, 14 is a high-temperature flue gas conveying pipeline, 15 is a flue gas heat exchanger, and 16 is a preheated air pipeline.
Detailed Description
Example 1
The embodiment provides a marine solid waste plasma gasification melting system, as shown in fig. 1, which comprises a feeding device, a plasma gasification melting chamber 4, a gasification combustion chamber 11 and a flue gas heat exchanger 15, wherein an output end of the feeding device is connected with a feeding hole of the plasma gasification melting chamber 4, a synthetic gas outlet of the plasma gasification melting chamber 4 is connected with a synthetic gas inlet of the gasification combustion chamber 11 through a synthetic gas conveying pipeline 7, and a flue gas outlet of the gasification combustion chamber 11 is connected with a flue gas inlet of the flue gas heat exchanger 15 through a high-temperature flue gas conveying pipeline 14. The feeding device comprises a bin 1, a spiral pusher 2 and a feeding chute 3, a double-roller crushing device is arranged at the bottom of the bin 1, the lower part of the bin 1 is connected with the spiral pusher 2, the tail part of the spiral pusher 2 is connected with the feeding chute 3, an external heating type drying device is arranged outside the spiral pusher 2 and the feeding chute 3, the spiral pusher 2 adopts an external heating mode to dry materials, the temperature of high-temperature flue gas used for heating is about 600 ℃, and the high-temperature flue gas comes from a flue gas heat exchanger 15. The external heating type drying device comprises a cylindrical shell, the shell is arranged outside the spiral pusher 2 and the feeding chute 3, an inlet of the shell is connected with a preheated air outlet of a flue gas heat exchanger 15 through a preheated air pipeline 16, an outlet of the shell is connected with the inside of the plasma gasification melting chamber 4, and the preheated air pipeline 16 is also connected with a high-temperature pump. An included angle of 35-55 degrees is formed between the feeding chute 3 and the plasma gasification melting chamber 4.
The plasma gasification melting chamber 4 is divided into an upper gasification zone 10 and a lower ash slag melting zone 9, wherein the gasification zone 10 adopts mullite refractory bricks with the thickness of 0.070m and mullite castable with the thickness of 0.03m as heat insulation materials, and the ash slag melting zone 9 adopts corundum materials for heat insulation and heat preservation, and the thickness is 0.05 m. The gasification zone 10 is provided with a feeding device and a synthesis gas circulation reflux device, and the bottom of the ash slag melting zone 9 is provided with a slag discharge port. Install 4 first plasma torches 6 on the slope in the lateral wall of handing-over department between ash fusion district 9 and gasification district 10, first plasma torch 6 adopts the frequency conversion direct current non-transfer arc plasma torch (purchase from imperial source science and technology company, the model is the DLZ type) that output is 100KW, installs 4 primary air inlet 5 on the slope of the lateral wall of gasification district 10, and first plasma torch 6, primary air inlet 5's slope installation angle are 35, and primary air inlet is equipped with first regulating valve. The synthesis gas circulation reflux device comprises a synthesis gas reflux pipe 8, a proportional flow valve is arranged on the synthesis gas reflux pipe 8, the synthesis gas reflux pipe 8 is connected with a synthesis gas reflux pump, the inlet of the synthesis gas reflux pipe 8 is connected with the upper synthesis gas outlet of the gasification area 10, and the outlet is connected with the lower synthesis gas inlet of the gasification area 10. During the working process of the plasma gasification melting chamber 4, coke and ash slag are melted in the ash slag melting zone 9, the synthesis gas is shunted in the gasification zone 10 through a draught fan arranged at the top of the plasma gasification melting chamber 4, one part of the synthesis gas returns to the lower part of the gasification zone 10 through a synthesis gas return pipe 8 to be combusted, and the other part of the synthesis gas directly enters a gasification combustion chamber 11 through a synthesis gas conveying pipeline 7.
The heat insulation material of the gasification combustion chamber 11 adopts aluminum silicate casting material and high-alumina refractory brick as heat insulation material, the thickness of the aluminum silicate casting material is 0.05m, and the thickness of the high-alumina refractory brick is 0.065 m. The top of the gasification combustion chamber 11 is provided with a second plasma torch 12, and the output power of the second plasma torch 12 is 35-50 KW. The side wall of the gasification combustion chamber 11 is obliquely provided with 4 secondary air inlets 13, the oblique installation angle of the secondary air inlets 13 is 35 degrees, and the secondary air inlets 13 are provided with second regulating valves. The lower part of the gasification combustion chamber 11 is provided with a synthetic gas inlet, the upper part is provided with a flue gas outlet, an induced draft fan is arranged at the position, located at the flue gas outlet, of the upper part of the gasification combustion chamber 11, the gasification combustion chamber 11 adopts a mode of downward inlet and upward outlet, and high-temperature flue gas is discharged from the top through the induced draft fan. During the operation of the gasification combustion chamber 11, the second plasma torch 12 is ignited, and the synthesis gas inside the second plasma torch is fully combusted under the combustion supporting effect of the air supplied by the secondary air inlet 13. The high-temperature flue gas after combustion in the gasification combustion chamber 11 enters the flue gas heat exchanger 15 through the high-temperature flue gas conveying pipeline 14 to preheat air.
The flue gas heat exchanger 15 comprises a housing having a flue gas inlet and a flue gas outlet and a heat exchange tube mounted within the housing having an air inlet and a preheated air outlet.
The solid waste material of the embodiment is ship IMO 02-grade domestic garbage, the water content of the garbage is 50%, the ash content is 7%, the lower calorific value is 10000kJ/kg, and the treatment capacity is 5 tons t/d. Before the system works, the solid waste on the ship is conveyed to the storage bin 1 in advance, and is crushed at the bottom of the storage bin 1 through a double-roller crushing device.
When the marine solid waste plasma gasification melting system works, the first plasma torch 6 is firstly opened to preheat the plasma gasification melting chamber 4, the first plasma torch 6 starts arc discharge under high pressure to ionize carrier gas air into high-density ionized gas, and meanwhile, the first plasma torch 6 is arranged obliquely downwards at 35 degrees to form uniform high-temperature ionized gas flow. Then, the primary air inlet 5 was opened by the first adjustment valve, and the air equivalence ratio in the plasma gasification melting chamber 4 was adjusted to 0.3. And when the temperature of the plasma gasification melting chamber 4 is raised to 1000 ℃ by the heat energy generated by the work of the first plasma torch 6, starting the spiral material pusher 2 to start feeding, continuously and uniformly feeding the crushed solid wastes into the gasification melting chamber 4 under the action of the spiral material pusher 2 to carry out pyrolysis gasification, and drying the wastes by the spiral material feeder 2 in an external heating mode during feeding. The gas production of the plasma gasification melting chamber 4 is stable after the system is started for about 30 minutes.
Adjusting a synthesis gas reflux pump on the synthesis gas reflux pipe 8 to ensure that the reflux proportion of the synthesis gas is 20-35%, and combustible components CO and H in the refluxed synthesis gas2、CH4Returning to the lower portion of the gasification zone 10 for combustion of the synthesis gas. Wherein the steam in the returned synthesis gas is supplemented to the gasification zone 10 as a gasifying agent, the amount of steam in the returned synthesis gas being about 10 kg/h. In the traditional method, 79% of nitrogen is brought in by using air as a gasifying agent, so that the calorific value and purity of the synthesis gas are reduced, and in the embodiment, the calorific value and purity of the synthesis gas can be improved by using steam as the gasifying agent. Then, the power of the first plasma torch 6 is adjusted so that the average temperature of the gasification zone 10 is 1100-1300 ℃ (generally about 1250 ℃), and the temperature of the ash slag melting zone 9 is 1400-1600 ℃ (generally about 1500 ℃). The coke and the ash are melted at high temperature, the carbon residue of the ash reacts completely, and the ash can be recycled as a building material, so that harmless treatment is really realized. In the high-temperature high-density oxygen-poor atmosphere, the carbon base is completely cracked instantly, the dioxin is thoroughly decomposed, and the NO is effectively restrained in the reductive atmosphereX，SO2And (4) forming.
The residual synthesis gas in the plasma gasification melting chamber 4 enters the gasification combustion chamber 11 through the synthesis gas conveying pipeline 7 to be fully combusted, particulate matters, tar and the like in the smoke are further removed, and the temperature of the gasification combustion chamber 11 is maintained to be more than 1200 ℃ during combustion. The air excess coefficient of the gasification combustion chamber 11 is adjusted to about 1.3 through a second adjusting valve, and secondary air is supplemented to the gasification combustion chamber 11 through a secondary air inlet 13. The calorific value of the synthetic flue gas generated after combustion is about 5000KJ/kg, and the calorific value of the synthetic flue gas can meet the requirement of self-sustaining combustion, so that the gasification combustion chamber 11 only needs to be provided with the second plasma torch 12 with lower power for auxiliary combustion and ignition starting, and 1 plasma torch (purchased from longyuan science and technology company, model number DLZ type) with output power of 45KW is arranged in the embodiment. The high-temperature flue gas outlet is arranged at the upper part of the gasification combustion chamber 11 and is connected with a flue gas heat exchanger 15 through a high-temperature flue gas conveying pipeline 14. Two media of air and flue gas are introduced into the flue gas heat exchanger 15 for heat exchange, the temperature of inlet flue gas of the flue gas heat exchanger 15 is 1200 ℃, the temperature of outlet flue gas after heat exchange is 200 ℃, the temperature of cold air is normal temperature (generally 20 ℃), and the temperature of the preheated air outlet after heating is 700 ℃. The preheated air dries the domestic garbage with the water content of 50 percent, oxygen is provided for the plasma gasification melting chamber 4 through the primary air inlet 5, and a gasifying agent is provided for the plasma gasification melting chamber 4 through the synthesis gas reflux circulation device. The preheated air is introduced into an external heating type drying device of the feeding device through a preheated air pipeline under the action of a high-temperature pump to indirectly dry the materials, and the flue gas of the flue gas heat exchanger is cooled to 200 ℃ after being subjected to heat exchange and quenching and is directly discharged through a flue gas outlet.
Adopt the utility model provides a marine solid useless plasma gasification melting system, the solid useless behind the drying evenly throws the entering plasma gas melting chamber in succession through the stoker. Under the condition of high temperature and oxygen deficiency in the gasification melting chamber, a vitreous product generated by melting inorganic substances can be used as a building material; organic matter in the solid waste is instantly gasified under the condition of high temperature and oxygen deficiency to generate low molecular combustible gas, the combustible gas enters a gasification combustion chamber to be fully combusted, heat energy released by combustion of the combustible gas is recycled to a material drying part through a flue gas heat exchanger, and tail gas is treated by a quenching system to avoid secondary generation of dioxin. The oxygen-deficient environment (air equivalent coefficient 0.2-0.3) in the gasification combustion chamber can inhibit NOXClean and excellent combustion of generated combustible gasThe characteristics reduce the smoke amount and pollutant generation amount compared with the direct incineration of solid waste. Compare with conventional marine solid useless processing system, the utility model discloses do not need fossil fuel combustion-supporting, alleviateed energy resource consumption, reduced the flue gas volume and the air contaminant that fossil burning produced simultaneously (see table 1, table 2 and table 3). The conventional marine incinerator has the burning temperature controlled at 850 deg.c, and can not decompose dioxin in solid waste and complete combustion of organic matter in solid waste, with ash containing 10% of unburnt matter. The utility model discloses in, through plasma torch high pressure arcing heating, under 1100 ~ 1500 ℃ high temperature oxygen deficiency condition, when the dioxin that will bring in decomposes, the regeneration of dioxin has been avoided to tail gas treatment end adoption rapid cooling technology. Under the high temperature environment of 1500 ℃ in an ash melting zone, inorganic matters are thoroughly innoxious to form a glass body.
TABLE 1 flue gas concentration for plasma gasification melting System
TABLE 2 flue gas amount comparison of plasma gasification melting system for ship and traditional incinerator for ship
| (Mode) | Amount of flue gas | Temperature of melting zone |
| Plasma gasification melting system | 3.4356（Nm3/kg garbage) | 1400～1600℃ |
| Traditional marine incinerator | 6.2～7.8（Nm3/kg garbage) | 850～1200℃ |
TABLE 3 detection of the result of melting and leaching (mg/L) of the plasma gasification melting system for ships
| Heavy metals | Cd | Pb | Cr6+ | As | Be | Ba | Ni | Cyanide compounds | Cr | Zn | Cu | Fluoride compounds | Hg |
| Slag of molten slag | ＜0.003 | ＜0.05 | ＜0.004 | ＜0.009 | ＜0.0003 | ＜0.004 | ＜0.01 | ＜0.004 | ＜0.01 | ＜0.014 | ＜0.01 | ＜0.05 | 0.6 |
| Emission standard | 0.3 | 3 | 0.05 | 0.01 | 0.1 | 100 | 10 | 1.5 | 10 | 50 | 50 | 50 | 0.05 |
As can be seen from tables 1 to 3, the concentration of the flue gas discharged from the plasma gasification melting system is far superior to the national standard, wherein dioxin and NO are containedXThe discharge amount of the catalyst reaches the international advanced level; plasma processThe emission of smoke of the sub-gasification melting system is about 50% of the emission of the traditional incinerator; ash and slag of the plasma gasification melting system are completely harmless, the leaching rate is lower than the international standard requirement, the ash and slag thermal ignition loss rate can reach 0.92 percent and is far lower than 10 percent of that of the marine incinerator; the energy consumption of the 200kg/h marine plasma direct gasification melting system is about 150KW, and the energy sources are all electric energy. Plasma torch type selection is 120-150 kw, and synthetic gas heat value is 8590KJ/m3By refluxing 38% of the syngas, 36% of the electricity consumption is saved.
In addition to the above embodiments, the present invention may have other embodiments. All the technical solutions formed by adopting equivalent substitutions or equivalent transformations fall within the protection scope claimed by the present invention.
Claims (10)
1. The utility model provides a marine solid useless plasma gasification melting system which characterized in that: the device comprises a feeding device, a plasma gasification melting chamber, a gasification combustion chamber and a flue gas heat exchanger, wherein the output end of the feeding device is connected with the feeding hole of the plasma gasification melting chamber, the synthetic gas outlet of the plasma gasification melting chamber is connected with the synthetic gas inlet of the gasification combustion chamber, and the flue gas outlet of the gasification combustion chamber is connected with the flue gas inlet of the flue gas heat exchanger; and a group of first plasma torches are uniformly arranged on the side wall of the plasma gasification melting chamber along the circumferential direction of the side wall, a synthesis gas circulating and refluxing device is arranged in the plasma gasification melting chamber, and a preheated air outlet of the flue gas heat exchanger is connected with an external heating type drying device arranged outside the feeding device through a preheated air pipeline.
2. The plasma gasification melting system for marine solid waste according to claim 1, wherein: the plasma gasification melting chamber is divided into a gasification area and an ash slag melting area, the feeding device and the synthesis gas circulating and refluxing device are arranged in the gasification area, and a slag discharge port is arranged at the bottom of the ash slag melting area.
3. The plasma gasification melting system for marine solid waste according to claim 2, characterized in that: 2-4 first plasma torches are obliquely arranged at the joint between the ash slag melting zone and the gasification zone, and 2-4 primary air inlets are obliquely arranged on the side wall of the gasification zone.
4. The marine solid waste plasma gasification melting system of claim 3, wherein: the inclined installation angles of the first plasma torch and the primary air inlet are both 35 degrees, the output power of the first plasma torch is 50-500 KW, and the primary air inlet is provided with a first adjusting valve.
5. The plasma gasification melting system for marine solid waste according to claim 2, characterized in that: the synthesis gas circulation reflux device comprises a synthesis gas reflux pipe, a proportional flow valve is arranged on the synthesis gas reflux pipe, the synthesis gas reflux pipe is connected with a synthesis gas reflux pump, the inlet of the synthesis gas reflux pipe is connected with the upper synthesis gas outlet of the gasification area, and the outlet is connected with the lower synthesis gas inlet of the gasification area.
6. The plasma gasification melting system for marine solid waste according to claim 2, characterized in that: the feeding device comprises a bin, a spiral pusher and a feeding chute, the lower part of the bin is connected with the spiral pusher, the tail part of the spiral pusher is connected with the feeding chute, and an external heating type drying device is arranged outside the spiral pusher.
7. The plasma gasification melting system for the marine solid waste is characterized in that: the external heating type drying device comprises a cylindrical shell, the shell is arranged outside the spiral material pusher, an inlet of the shell is connected with a preheated air outlet of the flue gas heat exchanger through a preheated air pipeline, an outlet of the shell is connected with the inside of the plasma gasification melting chamber, and the preheated air pipeline is connected with a high-temperature pump.
8. The plasma gasification melting system for marine solid waste according to claim 1, wherein: and a second plasma torch is arranged at the top of the gasification combustion chamber, and the output power of the second plasma torch is 35-50 KW.
9. The plasma gasification melting system for marine solid waste according to claim 8, wherein: 2 ~ 4 secondary air inlets are installed to the slope on the lateral wall of gasification combustion chamber, the secondary air inlet is equipped with second governing valve.
10. The plasma gasification melting system for marine solid waste according to claim 1, wherein: the flue gas heat exchanger comprises a shell and a heat exchange tube arranged in the shell, wherein the shell is provided with a flue gas inlet and a flue gas outlet, and the heat exchange tube is provided with an air inlet and a preheated air outlet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122106101.5U CN216005774U (en) | 2021-09-02 | 2021-09-02 | Marine solid waste plasma gasification melting system |
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