CN113583718A - Gasification and melting system and method for solid waste plasma for ship - Google Patents
Gasification and melting system and method for solid waste plasma for ship Download PDFInfo
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- CN113583718A CN113583718A CN202111025777.XA CN202111025777A CN113583718A CN 113583718 A CN113583718 A CN 113583718A CN 202111025777 A CN202111025777 A CN 202111025777A CN 113583718 A CN113583718 A CN 113583718A
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- 238000002309 gasification Methods 0.000 title claims abstract description 122
- 238000002844 melting Methods 0.000 title claims abstract description 109
- 230000008018 melting Effects 0.000 title claims abstract description 109
- 239000002910 solid waste Substances 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims description 12
- 239000007789 gas Substances 0.000 claims abstract description 129
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 110
- 239000003546 flue gas Substances 0.000 claims abstract description 110
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 93
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 92
- 238000002485 combustion reaction Methods 0.000 claims abstract description 86
- 238000009272 plasma gasification Methods 0.000 claims abstract description 75
- 239000002893 slag Substances 0.000 claims abstract description 22
- 238000001035 drying Methods 0.000 claims abstract description 17
- 238000010438 heat treatment Methods 0.000 claims abstract description 16
- 238000000197 pyrolysis Methods 0.000 claims abstract description 13
- 238000010992 reflux Methods 0.000 claims description 43
- 239000000463 material Substances 0.000 claims description 18
- 239000003795 chemical substances by application Substances 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 230000009471 action Effects 0.000 claims description 7
- 238000003860 storage Methods 0.000 claims description 6
- 238000009434 installation Methods 0.000 claims description 5
- 239000012159 carrier gas Substances 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 abstract description 15
- 238000009270 solid waste treatment Methods 0.000 abstract description 5
- 239000005416 organic matter Substances 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 description 16
- 230000002829 reductive effect Effects 0.000 description 13
- 239000010813 municipal solid waste Substances 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
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- YKTSYUJCYHOUJP-UHFFFAOYSA-N [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] Chemical compound [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] YKTSYUJCYHOUJP-UHFFFAOYSA-N 0.000 description 2
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- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
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- 239000000571 coke Substances 0.000 description 2
- KZHJGOXRZJKJNY-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Si]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O KZHJGOXRZJKJNY-UHFFFAOYSA-N 0.000 description 2
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
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- 239000002918 waste heat Substances 0.000 description 2
- 229910002975 Cd Pb Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
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- 239000010791 domestic waste Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000010891 electric arc Methods 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 150000002222 fluorine compounds Chemical class 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/154—Pushing devices, e.g. pistons
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0903—Feed preparation
- C10J2300/0909—Drying
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/12—Heating the gasifier
- C10J2300/123—Heating the gasifier by electromagnetic waves, e.g. microwaves
- C10J2300/1238—Heating the gasifier by electromagnetic waves, e.g. microwaves by plasma
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
- C10J2300/1628—Ash post-treatment
- C10J2300/1634—Ash vitrification
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
本发明涉及一种船用固废等离子气化熔融系统，包括进料装置、等离子气化熔融室、气化燃烧室和烟气换热器，所述进料装置的输出端与等离子气化熔融室的进料口相连，所述等离子气化熔融室的合成气出口与气化燃烧室的合成气入口相连，所述气化燃烧室的烟气出口与烟气换热器的烟气入口相连；在所述等离子气化熔融室的侧壁上沿其周向均匀设置有一组等离子炬，所述等离子气化熔融室设有合成气循环回流装置，所述烟气换热器的预热空气出口通过预热空气管路与设置在进料装置外的外热式干燥装置相连。本发明的优点是有效抑制了二噁英和NOX的生成，灰渣彻底无害化，有机物分解成可燃合成气，热解气化生成的可燃气的燃烧性能优于船上传统固废处理装置。
The invention relates to a plasma gasification and melting system for marine solid waste, comprising a feeding device, a plasma gasification and melting chamber, a gasification combustion chamber and a flue gas heat exchanger. The output end of the feeding device is connected to the plasma gasification and melting chamber. The feed port of the plasma gasification melting chamber is connected with the synthesis 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; A group of plasma torches are uniformly arranged on the side wall of the plasma gasification and melting chamber along its circumferential direction. The plasma gasification and melting chamber is provided with a synthesis gas circulation and return device. The preheated air outlet of the flue gas heat exchanger It is connected with the external heating drying device arranged outside the feeding device through the preheating air pipeline. The advantages of the invention are that the generation of dioxin and NOx is effectively suppressed, the ash and slag are completely harmless, the organic matter is decomposed into combustible synthesis gas, and the combustion performance of the combustible gas generated by pyrolysis gasification is better than that of the traditional solid waste treatment device on board.
Description
Technical Field
The invention belongs to the technical field of ship construction and incineration, relates to a ship solid waste treatment system, and particularly relates to a ship solid waste plasma gasification melting system and method, which can treat various mixed wastes.
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.
Disclosure of Invention
The technical problem to be solved by the invention is to overcome the defects of the prior art and provide a gasification and melting system and a gasification and melting method for solid waste plasma for ships.
In order to solve the technical problems, the invention provides 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 a feeding hole of the plasma gasification melting chamber, a synthetic gas outlet of the plasma gasification melting chamber is connected with a synthetic gas inlet of the gasification combustion chamber, and a flue gas outlet of the gasification combustion chamber is connected with a flue gas inlet of the 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 system combines the pyrolysis gasification technology with the high heat energy of the plasma torch, the solid waste on the ship is firstly gasified into combustible synthetic gas, the synthetic gas is fully combusted, ash and carbon residue are melted under the high temperature action of the plasma torch, the energy consumption required by the system is provided by the synthetic gas reflux and the plasma torch, and the consumption of fossil energy such as diesel oil is reduced. 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 marine solid waste treatment device provided by the invention mainly aims at cleaning treatment, and recovers part of synthesis gas and high-temperature flue gas waste heat, wherein the heat value of the synthesis gas is as high as 6000-15000 KJ/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 further optimized technical scheme of the invention is 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 structure, the synthesis gas at the upper part of the plasma gasification melting chamber is divided into two parts by the synthesis gas circulating reflux device, one part of the synthesis gas is refluxed to the gasification area of the plasma gasification melting chamber, and CO and H in the synthesis gas are2、CH4The heat required by the reaction is released by combustion, the power consumption required by pyrolysis and gasification can be reduced, and the water vapor in the backflow synthesis gas is used as a gasification agent to be supplemented to a gasification zone, compared with the pure air used as gasificationThe agent and the water vapor do not carry in nitrogen, 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 energy consumption required by the system of the invention is from plasma torch electric heating and partial combustion heat of the synthesis gas, other auxiliary heat sources such as diesel oil, coal, natural gas and the like are not needed, and fossil energy consumption and the amount of smoke generated by the fossil energy consumption are reduced.
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 a gasifying agent-steam. 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 mixing water and air as a gasifying agent is superior to the synthesis gas generated by only using air as the gasifying agent in the aspects of quality, cleanliness, synthesis efficiency and the like because 79 percent of N is brought in by the air gasifying agent2The 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 invention adopts a shell-and-tube gas-gas heat exchanger to preheat air, the temperature of the inlet and outlet of the flue gas is 1200 DEG/700 DEG, the temperature of the inlet and outlet of the air is normal temperature/650 DEG, the high-temperature flue gas is discharged after quenching to avoid the re-synthesis of dioxin, and the preheated air is used for drying the materials in an indirect heat exchange mode. 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 invention also provides a plasma gasification melting method for marine solid waste, which comprises the following steps:
firstly, starting a furnace, namely, a first plasma torch performs arc starting and discharging under high pressure, carrier gas air is ionized into high-density ionized gas, and the generated heat energy raises the temperature in a plasma gasification melting chamber to 1000-1600 ℃;
secondly, feeding, namely conveying the solid waste on the ship to a storage bin, and feeding the solid waste into a gasification melting chamber under the action of a spiral pusher for pyrolysis and gasification;
thirdly, pyrolysis gasification, namely adjusting the primary air equivalent ratio of the plasma gasification melting chamber to be 0.2-0.3, adjusting the power of the first plasma torch and the power of a synthesis gas reflux pump to ensure that the temperature of a gasification zone in the plasma gasification melting chamber is 1100-1300 ℃, the temperature of an ash slag melting zone is 1400-1600 ℃, and providing reflux synthesis gas containing a gasification agent for the plasma gasification melting chamber through the synthesis gas reflux pump, wherein the main component of the gasification agent is water vapor (also containing a small amount of air), and the volume ratio of the water vapor in the reflux synthesis gas is 16-34%;
step four, the synthesis gas is combusted, namely the synthesis gas in the gasification zone is introduced into a gasification combustion chamber for full combustion, an igniter of a second plasma torch is started, and the equivalent ratio of secondary air in the gasification combustion chamber is adjusted to be 1.3 so as to maintain the temperature of the gasification combustion chamber to be more than 1200 ℃;
and fifthly, flue gas heat exchange, namely introducing high-temperature flue gas in the gasification combustion chamber into a flue gas heat exchanger through a flue gas inlet, wherein the temperature at the flue gas inlet is 1200 ℃, the temperature at the flue gas outlet is 200 ℃, the temperature at the air inlet is normal temperature, the temperature at the preheated air outlet is 700 ℃, the preheated air is introduced into an external heating type drying device of a feeding device through a preheated air pipeline under the action of a high-temperature pump to indirectly dry the material, and the flue gas of the flue gas heat exchanger is cooled to 200 ℃ after being subjected to heat exchange and rapid cooling and is directly discharged through a flue gas outlet.
According to the invention, part of the synthesis gas in the gasification melting chamber flows back, so that the power consumption of the plasma torch is reduced, and the heat of the high-temperature flue gas is recycled to dry the material and serve as air, so that the heat required by gasification is reduced, and the treatment efficiency is improved. The smoke emission is reduced, meanwhile, smoke pollutants and plasma energy consumption are reduced, the combustion efficiency is improved, and the ash residue thermal ignition reduction rate is reduced.
The invention has the advantages that the oxygen-deficient environment of the plasma gasification melting chamber effectively inhibits dioxin and NOXThe plasma torch provides 1100-1600 ℃ high-temperature environment, so that dioxin is completely decomposed, ash is thoroughly harmless, 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 a traditional solid waste treatment device on a ship. The energy consumption required by the system of the invention is totally from electric energy, and the energy consumption of the plasma torch is slowed down through partial synthesis gas reflux and heat exchange of the flue gas heat exchanger, thereby solving the problems that the traditional marine incinerator needs to consume a large amount of fossil energy for auxiliary combustion, aggravates the energy consumption shortage, burns and burns the exhaust flue gas by fossil combustion, and the like. In addition, the flue gas after heat exchange by the flue gas heat exchanger is quenched to 200 ℃, so that the dioxin is avoided being resynthesized, the problems of insufficient combustion, secondary pollution of the flue gas, high ash residue burning rate, large flue gas amount and the like of the marine solid waste incinerator are solved, and the problem of high energy consumption of a plasma system is relieved.
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.
The working process of the marine solid waste plasma gasification melting system comprises five steps of furnace starting, feeding, pyrolysis and gasification, synthesis gas combustion, flue gas heat exchange and the like. Firstly, when a furnace is started, the first plasma torch 6 is 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 the generated heat energy can raise the temperature in the plasma gasification melting chamber to 1000-1600 ℃. Meanwhile, the first plasma torch 6 is arranged in a downward direction at an angle of 35 degrees in a tangential direction to form uniform high-temperature ionized air flow, the primary air inlet 5 is opened through the first adjusting valve, and the air equivalence ratio in the plasma gasification melting chamber 4 is adjusted to be 0.3. And (3) after the temperature of the plasma gasification melting chamber 4 is raised to 1000 ℃ by heat energy generated by the work of the first plasma torch 6, entering a feeding step, starting the spiral material pusher 2 to start feeding, crushing and conveying solid waste on the ship to a storage bin, continuously and uniformly entering the gasification melting chamber 4 under the action of the spiral material pusher 2 to carry out pyrolysis gasification, and drying the garbage 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.
During pyrolysis and gasification, the primary air equivalent ratio of the plasma gasification melting chamber 4 is adjusted to be 0.2-0.3, the power of the first plasma torch 6 and the power of a synthesis gas reflux pump are adjusted, so that the temperature of a gasification region 10 in the plasma gasification melting chamber 4 is 1100-1300 ℃, the temperature of an ash slag melting region 9 is 1400-1600 ℃, reflux synthesis gas containing a gasification agent is provided for the plasma gasification melting chamber 4 through the synthesis gas reflux pump, the gasification agent is composed of most of steam and a small part of air, and the volume ratio of the steam in the reflux synthesis gas is 16-34%. Specifically, a synthesis gas reflux pump on the synthesis gas reflux pipe 8 is adjusted to enable the reflux proportion of the synthesis gas to be 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 adjusting the power of the first plasma torch 6 to make the average temperature of the gasification zone 10 be 1100-1300The temperature of the ash melting zone 9 is 1400-1600 ℃ (generally 1500 ℃) which is about 1250 ℃. 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.
In the step of the synthesis gas combustion, the synthesis gas remained in the gasification zone 10 of the plasma gasification melting chamber 4 enters the gasification combustion chamber 11 through the synthesis gas conveying pipeline 7 for full combustion, an igniter of the second plasma torch 12 is started, the secondary air equivalence ratio of the gasification combustion chamber 11 is adjusted to be 1.3, the temperature of the gasification combustion chamber 11 is maintained to be more than 1200 ℃ during combustion, and particulate matters, tar and the like in the flue gas are further removed. 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.
In the flue gas heat exchange step, high-temperature flue gas in the gasification combustion chamber 11 is introduced into a flue gas heat exchanger 15 through a flue gas inlet, two media of the high-temperature flue gas and cold air are introduced into the flue gas heat exchanger 15 for heat exchange, the inlet flue gas temperature of the flue gas heat exchanger 15 is 1200 ℃, the outlet flue gas temperature of the flue gas heat exchanger is 200 ℃, the temperature of the entering cold air is normal temperature (generally 20 ℃), and the temperature of the outlet of the preheated air 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.
By adopting the system and the method for gasifying and melting the marine solid waste plasma, the dried solid waste is continuously and uniformly fed into the plasma gas melting chamber through the material pusher. 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 NOXThe generated fuel gas has clean and excellent combustion characteristics, and the flue gas amount and pollutant generation amount are reduced compared with the direct incineration of solid waste. Compared with the conventional marine solid waste treatment system, the system does not need fossil fuel for combustion supporting, reduces energy consumption, and simultaneously reduces the smoke amount and air pollutants generated by combustion of fossil fuel (see tables 1, 2 and 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. According to the invention, the plasma torch is used for high-pressure arc starting and heating, and the tail gas treatment end adopts a quenching process to avoid the regeneration of dioxin while the brought dioxin is decomposed at the high temperature of 1100-1500 ℃ under the anoxic condition. 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; the smoke emission of the plasma 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 technical solutions formed by adopting equivalent substitutions or equivalent transformations fall within the protection scope of the claims of 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: the top of the gasification combustion chamber is provided with a second plasma torch, the output power of the second plasma torch is 35-50 KW, 2-4 secondary air inlets are obliquely arranged on the side wall of the gasification combustion chamber, and second adjusting valves are arranged at the secondary air inlets.
9. 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.
10. A plasma gasification melting method for marine solid waste is characterized by comprising the following steps:
firstly, starting a furnace, namely, a first plasma torch performs arc starting and discharging under high pressure, carrier gas air is ionized into high-density ionized gas, and the generated heat energy raises the temperature in a plasma gasification melting chamber to 1000-1600 ℃;
secondly, feeding, namely conveying the solid waste on the ship to a storage bin, and feeding the solid waste into a gasification melting chamber under the action of a spiral pusher for pyrolysis and gasification;
thirdly, pyrolysis gasification, namely adjusting the primary air equivalent ratio of the plasma gasification melting chamber to be 0.2-0.3, adjusting the power of the first plasma torch and the power of a synthesis gas reflux pump to ensure that the temperature of a gasification zone in the plasma gasification melting chamber is 1100-1300 ℃, the temperature of an ash slag melting zone is 1400-1600 ℃, and providing reflux synthesis gas containing a gasification agent for the plasma gasification melting chamber through the synthesis gas reflux pump, wherein the main component of the gasification agent is water vapor, and the volume ratio of the water vapor in the reflux synthesis gas is 16-34%;
step four, the synthesis gas is combusted, namely the synthesis gas in the gasification zone is introduced into a gasification combustion chamber for full combustion, an igniter of a second plasma torch is started, and the equivalent ratio of secondary air in the gasification combustion chamber is adjusted to be 1.3 so as to maintain the temperature of the gasification combustion chamber to be more than 1200 ℃;
and fifthly, flue gas heat exchange, namely introducing high-temperature flue gas in the gasification combustion chamber into a flue gas heat exchanger through a flue gas inlet, wherein the temperature at the flue gas inlet is 1200 ℃, the temperature at the flue gas outlet is 200 ℃, the temperature at the air inlet is normal temperature, the temperature at the preheated air outlet is 700 ℃, the preheated air is introduced into an external heating type drying device of a feeding device through a preheated air pipeline under the action of a high-temperature pump to indirectly dry the material, and the flue gas of the flue gas heat exchanger is cooled to 200 ℃ after being subjected to heat exchange and rapid cooling and is directly discharged through a flue gas outlet.
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| CN114963200A (en) * | 2022-05-27 | 2022-08-30 | 中国船舶重工集团公司第七一一研究所 | Melting combustion type solid waste treatment device |
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