CN107723030B - Solid waste gasification system and gasification method thereof - Google Patents
Solid waste gasification system and gasification method thereof Download PDFInfo
- Publication number
- CN107723030B CN107723030B CN201711104502.9A CN201711104502A CN107723030B CN 107723030 B CN107723030 B CN 107723030B CN 201711104502 A CN201711104502 A CN 201711104502A CN 107723030 B CN107723030 B CN 107723030B
- Authority
- CN
- China
- Prior art keywords
- steam
- layer
- carbonization
- temperature
- solid waste
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000002910 solid waste Substances 0.000 title claims abstract description 95
- 238000002309 gasification Methods 0.000 title claims abstract description 93
- 238000000034 method Methods 0.000 title claims abstract description 30
- 238000003763 carbonization Methods 0.000 claims abstract description 88
- 238000001035 drying Methods 0.000 claims abstract description 81
- 230000007246 mechanism Effects 0.000 claims abstract description 69
- 239000002893 slag Substances 0.000 claims abstract description 52
- 238000000197 pyrolysis Methods 0.000 claims abstract description 50
- 230000009467 reduction Effects 0.000 claims abstract description 42
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 36
- 230000003647 oxidation Effects 0.000 claims abstract description 34
- 238000009826 distribution Methods 0.000 claims abstract description 29
- 239000007789 gas Substances 0.000 claims description 89
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 77
- 238000006243 chemical reaction Methods 0.000 claims description 52
- 238000007599 discharging Methods 0.000 claims description 31
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 26
- 230000005540 biological transmission Effects 0.000 claims description 18
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 16
- 239000002699 waste material Substances 0.000 claims description 16
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 15
- 239000001569 carbon dioxide Substances 0.000 claims description 13
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 13
- 239000000428 dust Substances 0.000 claims description 13
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 11
- 230000000630 rising effect Effects 0.000 claims description 11
- 238000007789 sealing Methods 0.000 claims description 10
- 239000007787 solid Substances 0.000 claims description 8
- 230000008569 process Effects 0.000 claims description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- 229910001385 heavy metal Inorganic materials 0.000 claims description 6
- 239000001257 hydrogen Substances 0.000 claims description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- 239000002918 waste heat Substances 0.000 claims description 4
- 239000004215 Carbon black (E152) Substances 0.000 claims description 3
- 229930195733 hydrocarbon Natural products 0.000 claims description 3
- 150000002430 hydrocarbons Chemical class 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 230000001174 ascending effect Effects 0.000 claims description 2
- 235000017166 Bambusa arundinacea Nutrition 0.000 claims 1
- 235000017491 Bambusa tulda Nutrition 0.000 claims 1
- 241001330002 Bambuseae Species 0.000 claims 1
- 235000015334 Phyllostachys viridis Nutrition 0.000 claims 1
- 239000011425 bamboo Substances 0.000 claims 1
- 238000005245 sintering Methods 0.000 abstract description 4
- 238000009270 solid waste treatment Methods 0.000 abstract description 3
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- 239000002956 ash Substances 0.000 description 42
- 238000006722 reduction reaction Methods 0.000 description 36
- 238000005516 engineering process Methods 0.000 description 13
- 239000003795 chemical substances by application Substances 0.000 description 11
- 239000010881 fly ash Substances 0.000 description 11
- 239000002737 fuel gas Substances 0.000 description 11
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 239000000463 material Substances 0.000 description 7
- 238000004056 waste incineration Methods 0.000 description 7
- 239000010813 municipal solid waste Substances 0.000 description 6
- 239000004449 solid propellant Substances 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 238000005728 strengthening Methods 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 239000000571 coke Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 239000002920 hazardous waste Substances 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 238000010079 rubber tapping Methods 0.000 description 3
- 238000007711 solidification Methods 0.000 description 3
- 230000008023 solidification Effects 0.000 description 3
- 241000282414 Homo sapiens Species 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000006870 function Effects 0.000 description 2
- 230000004927 fusion Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000002829 reductive effect Effects 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 241001465754 Metazoa Species 0.000 description 1
- PIYVNGWKHNMMAU-UHFFFAOYSA-N [O].O Chemical compound [O].O PIYVNGWKHNMMAU-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 239000002154 agricultural waste Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000010868 animal carcass Substances 0.000 description 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000011278 co-treatment Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 230000019771 cognition Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 210000003608 fece Anatomy 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 239000010805 inorganic waste Substances 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000002906 medical waste Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000010888 waste organic solvent Substances 0.000 description 1
- 238000004927 wastewater treatment sludge Methods 0.000 description 1
- 239000013585 weight reducing agent Substances 0.000 description 1
Classifications
-
- 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
-
- 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
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/725—Redox 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
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- 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
- C10J2300/16—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
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
The invention discloses a solid waste gasification system and a gasification method thereof. At present, solid waste treatment mainly comprises incineration, and secondary environmental pollution is easy to cause. The bottom of the furnace body is provided with an air distribution mechanism; the primary air inlet of the air distribution mechanism is communicated with the gasification fan through a one-way mixer, and the secondary air inlet is communicated with the inner cavity of the furnace body through an annular air duct and is also communicated with the air outlet of the one-way mixer; the mixed steam inlet of the unidirectional mixer is communicated with the high-temperature steam outlet; the furnace body is internally divided into an upper empty layer, a drying cavity, a carbonization cavity, a lower empty layer, a reduction cavity, an oxidation cavity and an ash cavity; the drying cavity is provided with a drying steam nozzle communicated with the high-temperature steam inlet, and the carbonization cavity is provided with a carbonization steam nozzle communicated with the high-temperature steam inlet; the high-temperature steam coil is arranged in the drying cavity and the carbonization cavity and is communicated with the high-temperature steam inlet and the high-temperature steam outlet; the upper empty layer is provided with a dry distillation gas outlet, and the lower empty layer is provided with a reducing gas outlet. The invention continuously converts solid waste into combustible gas and high-temperature sintering solidified slag, thereby achieving innocuity.
Description
Technical Field
The invention relates to a solid waste gasification system and a gasification method thereof, in particular to a solid waste gasification system based on high-temperature superheated steam strengthening reaction and a gasification method thereof.
Background
The solid waste, which is referred to as solid waste for short, refers to solid and semi-solid waste substances generated by human beings in production, consumption, living and other activities, and is commonly referred to as "garbage", and mainly comprises solid particles, garbage, slag, sludge, waste products, broken vessels, defective products, animal carcasses, spoiled foods, human and animal excreta and the like. Some countries also classify high concentration liquids such as waste acid, waste alkali, waste oil, waste organic solvents, etc. as solid waste.
Generally, the sources of solid waste are classified into municipal solid waste, industrial solid waste and agricultural waste; according to their composition, they can be classified into organic waste and inorganic waste; can be classified into harmful waste, general waste, etc. according to their pollution characteristics; in China, the method for preventing and treating the pollution of the solid waste is divided into urban solid waste, industrial solid waste and harmful waste.
The purpose of solid waste treatment is to achieve harmless, reduction and recycling, and the technology which is mature at present is an incineration technology.
The solid waste incineration is to oxidize and decompose combustible components in the solid waste into ash at high temperature. The incineration method has the advantages of high volume and weight reduction rate, high treatment speed, waste heat utilization and the like, but also has the following defects:
(1) Dioxin emission problem: cognition and fact that dioxin is generated by solid waste incineration are one of main factors causing 'adjacency', and thus difficult site selection and continuous group conflict events of solid waste incineration plants are caused; the solid waste incineration pollution control standard of various countries in the world also has a trend of further improvement, and the limit of the emission of dioxin in China is already 1ng TEQ/Nm at present 3 To 0.1 gTEQ/Nm 3 The method comprises the steps of carrying out a first treatment on the surface of the In the waste gas purification treatment process, part of dioxin is absorbed by activated carbon and fly ash and is trapped by a dust remover, and a small part of dioxin is discharged along with a chimney to cause secondary pollution;
(2) Malodor emission problem: the solid waste is sent into an incinerator for incineration, partial organic volatile gas is not completely incinerated due to the characteristics of fluctuation of the water content, character diversity, malodorous substances and the like of the solid waste, and the fume emission contains odor, especially in a rainy day with low air pressure, bad odor is diffused around a factory, complaints of surrounding residents are often caused, and the method is one of main factors causing 'adjacency';
(3) Fly ash disposal problem: the fly ash trapped by the dust remover is the 'sink' of dioxin and heavy metal, and the HW18 definitely incorporated into the national hazardous waste directory of 2016 edition burns and disposes the residue waste category; the method specifically comprises the following steps: "household garbage incineration fly ash" of waste code 772-002-18; "bottom slag, fly ash, and wastewater treatment sludge (excluding bottom slag generated by medical waste incineration disposal)" generated by disposal processes of hazardous waste incineration, pyrolysis, etc. of the waste code 772-003-18; "non-vitreous material and fly ash generated during disposal of hazardous waste plasma, high temperature melting, etc., of waste code 772-004-18"; waste code 772-005-18, "waste activated carbon generated by waste gas treatment in solid waste incineration process". The common technology for harmless treatment of fly ash is solidification landfill, cement kiln co-treatment, fusion solidification and the like, and various methods have extremely high cost.
The normal pressure moving bed (also called fixed bed) gasifying technology is to use air, air-water vapor, oxygen-water vapor and the like as gasifying agents to convert solid fuel into coal gas, wherein the solid fuel mainly comprises lignite, long flame coal, bituminous coal, anthracite, coke and the like. The whole gasification process is carried out under normal pressure; the fuel is added by the coal feeding device at the upper part of the movable bed, when the furnace burden is well loaded for gasification, the material layer in the furnace can be divided into six layers of belts, and the materials are respectively from top to bottom: empty layer, dry distillation layer, reduction layer, oxidation layer and ash layer; introducing a gasifying agent into the bottom, enabling fuel and the gasifying agent to flow reversely, gradually downwards moving the solid fuel along with the extension of reaction time in the gasifying furnace, and continuously discharging the solid fuel in the form of ash after the solid fuel passes through the drying, carbonization, reduction, oxidation and other stages; the operation method comprises a batch method and a continuous gasification method; air or oxygen-enriched air in the gasifying agent is used for reacting with carbon to provide heat, and water vapor is decomposed into gases such as hydrogen, carbon monoxide, carbon dioxide, methane and the like by utilizing the heat to react with the carbon; the active ingredients of the gasified gas mainly comprise H 2 CO and a small amount of CH 4 Industrial gas is generally classified into air gas, mixed gas (producer gas), water gas, semi-water gas and medium-heat value gas.
The furnace of the normal pressure moving bed gasification technology is in a reducing atmosphere, which is favorable for inhibiting dioxin and the existence of a high-temperature oxidation layer, so that the sintering and solidification of heavy metals are facilitated, and the process characteristics are increasingly attracting attention of environmental protection experts and are continuously tried in the solid waste disposal industry, but the problems are numerous:
(1) The water content of solid waste is often higher than that of coal and coke, the sensible heat of rising hot fuel gas only by a carbonization layer, a reduction layer and an oxidation layer is often insufficient, the oxidation layer is unstable, the heat value of the fuel gas is low, and stable flame combustion is difficult in a fuel gas boiler;
(2) In the normal pressure moving bed gasification technology, the temperature of an oxidation layer is up to 1000-1200 ℃, the temperatures of a reduction layer, a carbonization layer and a drying layer are gradually decreased layer by layer, so that the reduction reaction and the oxidation reaction of a gasification furnace are faster than the drying reaction and the carbonization reaction, solid waste is downwards moved to the reduction layer and the oxidation layer when the carbonization layer is insufficient for carbonization, the structural stability of the bed layers of the reduction layer and the oxidation layer is damaged, and the heat value of fuel gas is reduced;
(3) Because the furnace bottom is uneven in wind distribution and coking occurs at some time, the coke making operation intensity of operators is high, normal production is influenced, even the furnace is stopped, the furnace slag hot burning rate is high, and the requirement of the solid waste industry specification of less than 5% is not met;
(4) The normal pressure moving bed gasification technology has higher requirement on the granularity distribution of fuel, and because the solid waste has complex components and different shapes, and especially the solid waste gasification of a high material layer design, the reaction uniformity of each bed layer is poor, the workload of adjusting the temperature distribution of the bed layer by operators is large, the fluctuation of the heat value of gas is large, and the stable combustion of a gas boiler behind the furnace is influenced.
The normal pressure moving bed gasification technology is applied to solid waste disposal, so that secondary pollution caused by direct incineration of the solid waste is made up, and innovation of a solid waste gasification system and a gasification method thereof is urgently needed.
Disclosure of Invention
The invention aims at providing a solid waste gasification system and a gasification method based on high-temperature superheated steam strengthening reaction aiming at the problems that the prior solid waste treatment technology mainly uses incineration and is easy to cause secondary environmental pollution such as dioxin, malodor, heavy metal, fly ash discharge and the like. Due to the remarkable environment-friendly characteristic, the invention can be applied to urban solid waste and industrial solid waste, and can also be applied to harmless, reduction and recycling treatment of harmful waste.
The invention relates to a solid waste gasification system which comprises a top cover, a furnace body, a water jacket, a furnace skirt, a sealing feeding mechanism, an air distribution mechanism, a slag discharging mechanism, a carbonization gas outlet, a reduction gas outlet, a primary air inlet, a secondary air inlet, a downcomer interface, a steam riser interface, a carbonization barrel, a furnace wall, a high-temperature steam outlet and a high-temperature steam inlet, wherein the top cover is arranged on the furnace body; the furnace wall is built in the furnace body; the top of the furnace body is provided with a top cover, and the bottom and an ash tray of the slag discharging mechanism form a revolute pair; a sealing feeding mechanism is arranged on the top cover; a primary air inlet of the air distribution mechanism is communicated with a gasification air main pipe through an air pipeline, the gasification air main pipe is communicated with an air outlet of a one-way mixer, and an air inlet of the one-way mixer is communicated with a gasification fan through an air pipeline; the mixed steam inlet of the unidirectional mixer is communicated with the high-temperature steam outlet through a steam pipeline; the water jacket is positioned at the lower part of the furnace body; one end of a secondary air inlet of the air distribution mechanism is communicated with an annular air duct in the water jacket, and the other end of the secondary air inlet is communicated with the gasification air header through a secondary air header; the annular air duct is communicated with the inner cavity of the furnace body; the furnace wall in the middle of the furnace body is provided with an inner lug which is fixed with the carbonization barrel; the carbonization cylinder is a cylinder with the top and the bottom both open; the cavity formed by the top surface of the inner lug, the top surface of the dry distillation cylinder, the inner surface of the top cover and the inner surface of the furnace wall is divided into an upper empty layer and a drying cavity, and the upper empty layer is positioned at the upper part of the drying cavity; a carbonization gas outlet is arranged at the upper part of the upper empty layer; the inner cavity of the carbonization barrel is a carbonization cavity; the cavity formed by the bottom surface of the inner lug, the inner surface of the furnace body, the outer surface of the carbonization barrel and the top surface of the ash tray is divided into a lower empty layer, a reduction cavity, an oxidation cavity and an ash cavity which are arranged from top to bottom; the lower empty layer is provided with a reducing gas outlet at the upper part. The drying cavity is provided with a plurality of drying steam nozzles, and the drying steam nozzles are communicated with the high-temperature steam inlet through a steam pipeline; the carbonization cavity is provided with a plurality of carbonization steam nozzles, and the carbonization steam nozzles are communicated with a high-temperature steam inlet through a steam pipeline; the high-temperature steam coil is arranged in the drying cavity and the carbonization cavity, and is communicated with the high-temperature steam inlet and the high-temperature steam outlet through the steam pipeline, and the high-temperature steam inlet is communicated with high-temperature superheated steam equipment arranged outside the furnace body through the steam pipeline.
The high-temperature superheated steam equipment, the high-temperature steam coil pipe, the drying steam nozzle, the carbonization steam nozzle, the unidirectional mixer and the steam pipeline form a high-temperature superheated steam enhanced reaction system.
The high-temperature superheated steam equipment adopts a gas boiler, a waste heat boiler or a heat exchanger. The air distribution mechanism adopts a grate or a hood.
The slag discharging mechanism comprises an ash discharging transmission mechanism and an ash tray driven by the ash discharging transmission mechanism; the ash discharging transmission mechanism adopts hydraulic transmission, worm and gear transmission or gear transmission; the ash tray consists of a small ash knife for assisting ash discharge and a large ash knife for directly discharging ash.
The sealing feeding mechanism is a bell jar feeder, a hydraulic pushing mechanism, an air lock or a screw conveyor.
The unidirectional mixer consists of a unidirectional valve and a mixer; the one-way valve is arranged at the outlet of the fan; the mixed steam inlet of the unidirectional mixer is provided with a control valve.
The upper part and the lower part of the water jacket are respectively provided with a steam rising pipe interface and a descending pipe interface; the descending pipe joint is communicated with the steam collector through a water pipeline; the steam rising pipe joint is communicated with the steam collector through a steam pipeline; the steam collector is communicated with high-temperature superheated steam equipment through a steam pipeline; the water replenishing of the steam collector is softened water. The temperature of the high-temperature superheated steam is 500-1000 ℃ and the pressure is 0-294 KPa.
According to the gasification method of the solid waste gasification system, solid waste is sent into a furnace body through a sealed feeding mechanism, and a drying layer, a carbonization layer, a reduction layer, an oxidation layer and a ash slag layer are formed in the furnace body, wherein the gasification method comprises the following specific processes:
the solid waste is sent into the furnace body through the sealed feeding mechanism, air required by gasification is mixed with steam fed by the mixed steam inlet in the unidirectional mixer arranged on the outlet pipeline of the gasification fan to form gasification wind, the gasification wind is sent into the gasification wind main pipe, and then the gasification wind is divided into two paths to be sent into the furnace body, wherein one path reaches the wind distribution mechanism positioned at the bottom of the furnace body through the primary wind inlet, and the other path reaches the annular wind channel positioned in the water jacket through the secondary wind inlet, and then enters the side part of the furnace body. The gasified wind absorbs sensible heat of the ash slag layer and then heats up, and the semicoke formed by the oxidation layer and the reduction layer has exothermic reaction; the heavy metals in the solid waste are sintered and solidified after the reaction, ash becomes slag and moves down to an ash layer, and the gas generated after the reaction comprises carbon monoxide, carbon dioxide and water vapor. The slag is driven by the power of the slag discharging mechanism to rotate and move downwards while being cooled, the slag is rubbed with the inner surface of the furnace skirt below the furnace body, the massive slag is crushed, and the crushed and cooled slag is discharged out of the furnace body through the slag discharging mechanism. The gas generated by the oxidation layer rises to the reduction layer, the water vapor reacts with solid waste after carbonization, and the solid comprises semicoke in substances generated after the reaction, and the reduction gas comprises carbon monoxide, carbon dioxide, hydrogen and methane. Part of the reducing gas rises to the lower empty layer, and part of the dust carried by the reducing gas is settled and discharged from the reducing gas outlet; the other part rises to the dry distillation layer and the dry layer. The softened water is conveyed into a steam collector under pressure through a water pipeline, flows to a descending pipe joint through the water pipeline and flows into a water jacket, the softened water in the water jacket is heated into a steam-water mixture by heat transmitted by a furnace body, is discharged through a steam ascending pipe joint, and rises along the steam pipeline to reach the steam collector for steam-water separation, so that a water jacket and steam-water natural circulation system of the steam collector is formed; saturated steam is discharged out of the steam collector and reaches high-temperature superheated steam equipment through a steam pipeline, is heated into high-temperature superheated steam, and enters a high-temperature steam inlet through the steam pipeline. The steam at the high-temperature steam inlet is sent into the furnace body in three ways through a steam pipeline, wherein one way passes through the high-temperature steam coil pipe, and after heating the drying layer and the dry distillation layer, the steam is discharged from the high-temperature steam outlet and is communicated with the mixed steam inlet through the steam pipeline; the other path of the waste solid is sprayed into the drying layer through a drying steam nozzle through a steam pipeline, the temperature of the solid waste containing the moisture is raised, the solid waste is dehydrated, namely, the drying reaction is carried out, and part of the solid waste is subjected to the carbonization reaction, the drying tail gas after the drying reaction comprises steam, methane, carbon dioxide and nitrogen, and the solid waste after the drying reaction leaves the drying layer and moves to the carbonization layer; the third path is sprayed into the carbonization layer through a steam pipeline through a carbonization steam nozzle, and the carbonization reaction is carried out on the solid waste dried by the drying layer, the gas after the carbonization reaction comprises carbon monoxide, carbon dioxide, gaseous hydrocarbon and tar, and the solid waste after the carbonization reaction leaves the carbonization layer and moves to the reduction layer. The dry distillation gas generated by the dry distillation layer and the dry tail gas generated by the dry layer rise to the upper empty layer, and part of dust carried by the dry distillation layer is settled and discharged from a dry distillation gas outlet.
The discharge temperature of the dry distillation gas outlet is 100-300 ℃ and the pressure is 100-4000 Pa; the discharge temperature of the reducing gas outlet is 300-600 ℃ and the pressure is 500-5000 Pa.
The temperature range of the drying layer is 100-300 ℃, the temperature range of the dry distillation layer is 300-650 ℃, the temperature range of the reduction layer is 550-1000 ℃, the temperature range of the oxidation layer is 1000-1200 ℃, and the temperature range of the ash layer is 100-1000 ℃.
Compared with the prior art, the invention has the following beneficial effects:
(1) According to the invention, the drying steam nozzle is arranged on the drying layer, the high-temperature superheated steam sprayed out of the drying steam nozzle directly heats the solid waste, the solid waste containing moisture is rapidly heated and dehydrated, and part of the solid waste is subjected to carbonization reaction, so that the solid waste can adapt to fluctuation of higher moisture content of the solid waste entering the furnace.
(2) According to the invention, the dry distillation steam nozzle is arranged on the dry distillation layer, and the solid waste dried by the drying layer and the high-temperature superheated steam sprayed by the dry distillation steam nozzle directly react to generate combustible gas, so that the dry distillation reaction is enhanced, and the method can be suitable for stable gasification of the solid waste with lower carbon content.
(3) According to the invention, the steam coil is arranged on the drying layer and the dry distillation layer, the drying layer and the dry distillation layer are indirectly heated, the carbon monoxide, hydrogen and methane contents of the fuel gas components are further increased, the heat value of the fuel gas is high, and stable flame combustion can be achieved in the fuel gas boiler.
(4) According to the invention, the steam coil is arranged on the drying layer and the dry distillation layer, the temperature of high-temperature superheated steam tail gas discharged from the high-temperature steam outlet is more than 150 ℃, the high-temperature superheated steam still has a high enthalpy value, and the mixed steam inlet which is communicated with the unidirectional mixer through the steam pipeline is used as a gasifying agent to be consumed by the system, so that the heat energy utilization rate is remarkably improved.
(5) The invention is provided with the secondary air inlet and the annular air duct is arranged in the water jacket, solid waste in the furnace not only receives axial air distribution from the bottom air distribution mechanism, but also receives longitudinal air distribution from the annular air duct in the oxidation layer, thereby effectively solving the problem of uniform air distribution of the gasification furnace, effectively overcoming the coking problem of the oxidation layer and the ash slag layer in the furnace, and ensuring that the burning rate of the slag is lower than 5 percent and meeting the requirements of industry specifications.
(6) The carbonization gas outlet and the reduction gas outlet are respectively arranged at the upper part and the middle part of the furnace body, so that the system resistance is low, the reaction of each bed layer is uniform, the power consumption of the gasification fan is low, and the energy-saving effect of the system is improved; therefore, the contradiction of wide particle size distribution, high bed resistance and uneven air distribution of the solid waste fuel is solved, and the raw material adaptability is further enhanced.
(7) The invention solves the contradiction problem that the reduction reaction and the oxidation reaction of the gasification furnace are faster than the drying reaction and the carbonization reaction, the carbonization barrel is arranged in the middle of the furnace body, the thickness of the drying layer and the carbonization layer is increased, the further heating of high-temperature superheated steam is assisted, the reaction residence time of the drying and the carbonization is prolonged, the reaction residence time is more in line with the characteristic of solid waste gasification, and the system reaction stability is good.
(8) The medium participating in the strengthening reaction of the drying layer and the carbonization layer is high-temperature superheated steam, and the system has high safety and reliability due to the fusion of the steam to the reducing atmosphere in the gasification furnace.
(9) According to the invention, solid waste is continuously fed into the gasification furnace through the sealed feeding mechanism, a special drying layer, a carbonization layer, a reduction layer, an oxidation layer and an ash slag layer of the normal pressure moving bed gasification furnace are formed in the gasification furnace, oxygen in the gasification agent is reacted at a high temperature in the oxidation layer, and the drying layer, the carbonization layer and the reduction layer above the oxidation layer are in a reducing atmosphere, so that the generation of dioxin is effectively inhibited.
(10) The invention solves the problem of malodor of solid waste slag. The temperature of the oxidation layer reaches 1000-1200 ℃, the slag is high-temperature sintering solidified slag without volatile matters, and the problem of malodor caused by slag "clamping" of the conventional incineration technology is solved.
(11) The invention solves the problem of malodor emission of flue gas. Volatile matters in the solid waste are thoroughly volatilized and decomposed into one of components of fuel gas in a drying layer, a carbonization layer and a reduction layer, a small amount of malodorous components generated by gasification of the solid waste are odorized by combustible gas, and the odorization is one of safety measures in the fuel gas industry; the gas is sent to a gas boiler matched with the gas boiler to be burnt at high temperature, the temperature of a hearth and the residence time of the gas are designed according to the requirements of industry specifications, and various combustible components in the gas can be thoroughly incinerated to form the gas; the flue gas is sent to a subsequent flue gas purification facility to remove dust, sulfur dioxide and nitrogen oxides and then is discharged after reaching the standard.
(12) The invention solves the problem of fly ash discharge in solid waste disposal. The solid is reacted in the gasification furnace through three stages of a drying layer, a carbonization layer and a reduction layer to form semicoke, a small amount of generated dust is wrapped by materials from the carbonization layer and the drying layer above, the material layer is blocked and settled and slowly moves down to an oxidation layer, the temperature of the oxidation layer reaches 1000-1200 ℃, and fly ash is rapidly sintered and solidified at high temperature to form coarse-grained slag; the gasification furnace is provided with an empty layer, and the gas is settled through the upper empty layer and the lower empty layer before being discharged out of the gasification furnace, so that gas dust entrainment can be further reduced, and the dust settled in the empty layer is participated in the gasification reaction in the furnace again; the small amount of dust discharged from the gasifier along with the fuel gas is burnt at high temperature by the fuel gas boiler to become fly ash, which is captured by the subsequent flue gas purification facilities and returned to the system as solid waste raw materials, thus achieving ash-free emission.
Drawings
FIG. 1 is a schematic diagram of the system architecture of the present invention;
FIG. 2 is a cross-sectional view A-A of FIG. 1;
FIG. 3 is a schematic illustration of the connection of a high temperature steam coil to a high temperature steam outlet and a high temperature steam inlet in accordance with the present invention.
In the figure: 1. top cap, 2, dry distillation gas outlet, 3, dry layer, 4, furnace body, 5, dry steam nozzle, 6, lower empty layer, 7, dry distillation cylinder, 8, dry distillation steam nozzle, 9, dry distillation layer, 10, water jacket, 11, oxide layer, 12, mixed steam inlet, 13, gasification fan, 14, unidirectional mixer, 15, gasification wind header, 16, primary wind inlet, 17, wind distribution mechanism, 18, slag discharging mechanism, 19, furnace skirt, 20, ash layer, 21, downcomer interface, 22, secondary wind inlet, 23, steam riser interface, 24, reduction layer, 25, furnace wall, 26, reduction gas outlet, 27, high temperature steam outlet, 28, high temperature steam inlet, 29, upper empty layer, 30, sealing feeding mechanism.
Detailed Description
The invention is further described below with reference to the accompanying drawings.
As shown in fig. 1, 2 and 3, a solid waste gasification system comprises a top cover 1, a furnace body 4, a water jacket 10, a furnace skirt 19, a sealing feeding mechanism 30, a wind distributing mechanism 17, a slag discharging mechanism 18, a carbonization gas outlet 2, a reduction gas outlet 26, a primary wind inlet 16, a secondary wind inlet 22, a downcomer interface 21, a steam rising pipe interface 23, a carbonization barrel 7, a furnace wall 25, a high-temperature steam outlet 27 and a high-temperature steam inlet 28; the furnace wall 25 is built in the furnace body 4, and belongs to the category of furnace building technology in the prior art. The top of the furnace body 4 is provided with a top cover 1, and the bottom and an ash tray of the slag discharging mechanism 18 form a revolute pair; a sealing feeding mechanism 30 is arranged on the top cover 1; a wind distribution mechanism 17 is arranged above the slag discharging mechanism 18, a primary wind inlet 16 of the wind distribution mechanism 17 is communicated with a gasification wind main pipe 15 through a wind pipeline, the gasification wind main pipe 15 is communicated with a gas outlet of a one-way mixer 14, and an air inlet of the one-way mixer 14 is communicated with a gasification fan 13 through a wind pipeline; the mixed steam inlet 12 of the unidirectional mixer 14 is communicated with the high-temperature steam outlet 27 through a steam pipeline; sealing treatment is adopted at the primary air inlet 16; the water jacket 10 is positioned at the lower part of the furnace body 4; one end of a secondary air inlet 22 of the air distribution mechanism 17 is communicated with an annular air duct positioned in the water jacket 10, and the other end is communicated with the gasification air header 15 through a secondary air header; the annular air duct is communicated with the inner cavity of the furnace body 4; the furnace wall 25 in the middle of the furnace body 4 is provided with an inner convex block which is fixed with the carbonization barrel 7; the carbonization barrel 7 is a cylinder with the top and the bottom both open; the cavity formed by the top surface of the inner lug, the top surface of the carbonization barrel, the inner surface of the top cover 1 and the inner surface of the furnace wall 25 is divided into an upper empty layer 29 and a drying cavity, and the upper empty layer 29 is positioned at the upper part of the drying cavity; the upper empty layer 29 is provided with a carbonization gas outlet 2 at the upper part; the inner cavity of the carbonization barrel 7 is a carbonization cavity; the cavity formed by the bottom surface of the inner lug, the inner surface of the furnace body 4, the outer surface of the carbonization barrel 7 and the top surface of the ash tray is divided into a lower empty layer 6, a reduction cavity, an oxidation cavity and an ash cavity which are arranged from top to bottom; the lower empty layer 6 is provided with a reducing gas outlet 26 at an upper position. The drying cavity is provided with a plurality of drying steam nozzles 5, and the drying steam nozzles 5 are communicated with a high-temperature steam inlet 28 through a steam pipeline; the carbonization cavity is provided with a plurality of carbonization steam nozzles 8, and the carbonization steam nozzles 8 are communicated with a high-temperature steam inlet 28 through a steam pipeline; the high-temperature steam coil is arranged in the drying cavity and the carbonization cavity, and is communicated with the high-temperature steam inlet 28 and the high-temperature steam outlet 27 through a steam pipeline, and the high-temperature steam inlet 28 is communicated with high-temperature superheated steam equipment arranged outside the furnace body 4 through a steam pipeline; namely, the high-temperature superheated steam equipment is respectively delivered to the drying steam nozzle 5, the carbonization steam nozzle 8 and the high-temperature steam outlet 27 through three paths of high-temperature steam inlets 28; the high-temperature superheated steam equipment, the high-temperature steam coil pipe, the drying steam nozzle 5, the carbonization steam nozzle 8, the unidirectional mixer 14, the steam pipeline and the valve form a high-temperature superheated steam enhanced reaction system; the high-temperature superheated steam equipment adopts mature technology, such as a gas boiler, a waste heat boiler or a heat exchanger and the like. Solid waste is sent into the furnace body 4 through the sealing feeding mechanism 30 to form a drying layer 3 (positioned in a drying cavity), a carbonization layer 9 (positioned in a carbonization cavity), a reduction layer 24 (positioned in a reduction cavity), an oxidation layer 11 (positioned in an oxidation cavity) and an ash layer 20 (positioned in an ash cavity) which are special for the normal pressure moving bed gasification furnace;
the air distribution mechanism 17 is an even air distribution device adopting mature technology in the industries of grate, hood and the like.
The slag discharging mechanism 18 comprises an ash discharging transmission mechanism and an ash tray driven by the ash discharging transmission mechanism; the ash discharging transmission mechanism adopts mature technology, such as hydraulic transmission, worm and gear transmission or gear transmission; the ash tray for bearing the slag is a mature product and consists of a small ash knife for assisting ash discharging and a large ash knife for directly discharging ash; the tapping mechanism 18 may be designed for dry tapping or wet tapping depending on the material and engineering requirements.
The seal feeding mechanism 30 is one of feeding and conveying machines such as a bell jar feeder, a hydraulic pushing mechanism, a gas locker, a screw conveyor and the like.
The unidirectional mixer 14 consists of a unidirectional valve and a mixer; the one-way valve is arranged at the outlet of the fan to prevent gasifying agent in the gasifying air main pipe 15 from flowing backwards, and has the function of a check valve; a mixed steam inlet of the unidirectional mixer is provided with a control valve; the function of the mixer is to thoroughly mix the steam with the air. The gasifying fan 13 controls the supply of air or oxygen and the control of the supply of water vapor by combining with the mixed vapor inlet 12 of the unidirectional mixer 14, thereby controlling the gasifying agent to be one of air, mixed gas of air and water vapor and mixed gas of oxygen and water vapor. The gasifying agent in this embodiment is a mixed gas of air and water vapor.
The upper part and the lower part of the water jacket 10 are respectively provided with a steam rising pipe interface 23 and a falling pipe interface 21; the downcomer interface 21 is communicated with the steam collector through a water pipeline; the steam rising pipe interface 23 is communicated with the steam collector through a steam pipeline; the steam of the steam collector is communicated with high-temperature superheated steam equipment through a steam pipeline, saturated steam is heated into high-temperature superheated steam, and the high-temperature superheated steam is communicated with a high-temperature steam inlet 28 through the steam pipeline; the water replenishing of the steam collector is softened water.
The gasification method of the solid waste gasification system comprises the following specific steps:
solid waste is sent into the furnace body 4 through the sealed feeding mechanism 30, air required by gasification is pressurized by the gasification fan 13, and then uniformly mixed with steam fed by the mixed steam inlet 12 in the unidirectional mixer 14 arranged on the outlet pipeline of the gasification fan 13 to form gasification wind, the gasification wind is sent into the gasification wind main pipe 15, and then is divided into two paths to be sent into the furnace body 4, wherein one path reaches the wind distribution mechanism 17 positioned at the bottom of the furnace body 4 through the primary wind inlet 16, and the other path reaches the annular wind channel positioned in the water jacket 10 through the secondary wind inlet 22, and then enters the side part of the furnace body 4. The gasified wind absorbs the sensible heat of the ash layer 20 and then heats up, and a severe exothermic reaction occurs in semicoke formed by the oxidation layer 11 and the reduction layer 24; the heavy metals in the solid waste are sintered and solidified after the reaction, ash becomes slag and moves down to the ash layer 20, and the gas components generated after the reaction are mainly carbon monoxide, carbon dioxide and water vapor. Because the temperature of the oxide layer 11 is high, a water jacket 10 is arranged at the furnace body 4 part in the high temperature area for the purpose of preventing slag from melting and protecting the furnace wall 25, and a downcomer interface 21 is communicated with a steam collector through a water pipeline; the steam rising pipe interface 23 is communicated with the steam collector through a steam pipeline; the steam of the steam collector is heated by high-temperature superheated steam equipment to generate high-temperature superheated steam, and the water replenishing of the steam collector is softened water. The high-temperature slag is driven by the power of the slag discharging mechanism 18 to cool and slowly rotate downwards, continuously rubs against the inner surface of the skirt 19 below the furnace body 4, and large blocks of slag are crushed, so the skirt 19 is also called a slag crushing ring, and the crushed and cooled slag is discharged out of the furnace body 4 by the slag discharging mechanism 18. The high-temperature gas generated by the oxidation layer 11 rises to the reduction layer 24, water vapor and solid waste after carbonization react with each other to generate water gas, and the solid component is mainly semicoke and the reduction gas component is mainly carbon monoxide, carbon dioxide, hydrogen and methane in the substances generated after the reaction. A part of the reducing gas rises to the lower empty layer 6, and most of the dust carried by the reducing gas is settled and discharged from the reducing gas outlet 26; the other part rises to the dry distillation layer 9 and the dry distillation layer 3 to participate in the dry distillation reaction and the drying reaction. The softened water is pressed into a steam collector through a water pipeline, flows to a downcomer interface 21 through the water pipeline and flows into a water jacket 10, the softened water in the water jacket 10 is heated into a steam-water mixture by heat transmitted by a furnace body, is discharged through a steam rising pipe interface 23, and rises along the steam pipeline to reach the steam collector for steam-water separation, so that a water jacket and steam-water natural circulation system of the steam collector is formed; the saturated steam exits the steam collector through a steam line to a high temperature superheated steam unit, where it is heated to high temperature superheated steam, which enters the high temperature steam inlet 28 through a steam line. The high-temperature superheated steam is sent into the furnace body 4 in three paths through a steam pipeline from a high-temperature steam inlet 28, one path passes through a high-temperature steam coil pipe, and is discharged from a high-temperature steam outlet 27 after indirectly heating the drying layer 3 and the dry distillation layer 9, and is communicated with a mixed steam inlet 12 through the steam pipeline; the other path is sprayed into the drying layer 3 through a drying steam nozzle 5 by a steam pipeline, the solid waste containing moisture is quickly heated and dehydrated, namely, the drying reaction is carried out, and part of the solid waste is subjected to carbonization reaction, the drying tail gas component mainly comprises steam, methane, carbon dioxide and nitrogen, and the solid waste after the drying reaction slowly moves to the carbonization layer 9 from the drying layer 3; the third path is sprayed into the dry distillation layer 9 through a steam pipeline through a dry distillation steam nozzle 8, and dry distillation reaction is carried out on the solid waste dried by the drying layer 3, the gas components mainly comprise carbon monoxide, carbon dioxide, gaseous hydrocarbon and tar, and the solid waste after the dry distillation reaction slowly moves to the reduction layer 24 after leaving the dry distillation layer 9. The dry distillation gas generated by the dry distillation layer 9 and the dry tail gas generated by the dry distillation layer 3 rise to the upper empty layer 29, and most of the dust carried by the dry distillation gas is settled and discharged from the dry distillation gas outlet 2.
Thus, solid waste is continuously fed into the furnace body 4 through the sealed feeding mechanism 30, a drying layer 3, a carbonization layer 9, a reduction layer 24, an oxidation layer 11 and an ash layer 20 which are special for the moving bed gasification furnace are formed in the furnace, one part of gasifying agent (air and steam) is axially fed into the air distribution mechanism 17 at the bottom of the furnace body 4, and the other part of gasifying agent is longitudinally fed into the furnace body 4 through an annular air duct in the water jacket 10, and under the direct and indirect strengthening reaction of high-temperature superheated steam on the drying layer 3 and the carbonization layer 9, the solid waste is continuously converted into combustible gas and high-temperature sintering solidified slag, so that the harmless, reduction and recycling of solid waste disposal are achieved.
The temperature of the high-temperature superheated steam is 500-1000 ℃ and the pressure is 0-294 KPa.
The discharge temperature of the dry distillation gas outlet 2 is 100-300 ℃ and the pressure is 100-4000 Pa.
The discharge temperature of the reducing gas outlet 26 is 300 to 600 ℃ and the pressure is 500 to 5000Pa.
The temperature range of the drying layer 3 is 100-300 ℃, the temperature range of the dry distillation layer 9 is 300-650 ℃, the temperature range of the reduction layer 24 is 550-1000 ℃, the temperature range of the oxidation layer 11 is 1000-1200 ℃, and the temperature range of the ash layer 20 is 100-1000 ℃.
The examples are preferred embodiments of the present invention, but the present invention is not limited to the above-described embodiments, and any obvious modifications, substitutions or variations that can be made by one skilled in the art without departing from the spirit of the present invention are within the scope of the present invention.
Claims (10)
1. The utility model provides a solid waste gasification system, includes top cap, furnace body, water jacket, stove skirt, sealed feed mechanism, wind distribution mechanism, slag discharging mechanism, dry distillation gas outlet, reducing gas outlet, primary air inlet, overgrate air inlet, downcomer interface, steam rising pipe interface, dry distillation section of thick bamboo, furnace wall, high temperature steam outlet and high temperature steam inlet, its characterized in that: the furnace wall is built in the furnace body; the top of the furnace body is provided with a top cover, and the bottom and an ash tray of the slag discharging mechanism form a revolute pair; a sealing feeding mechanism is arranged on the top cover; a primary air inlet of the air distribution mechanism is communicated with a gasification air main pipe through an air pipeline, the gasification air main pipe is communicated with an air outlet of a one-way mixer, and an air inlet of the one-way mixer is communicated with a gasification fan through an air pipeline; the mixed steam inlet of the unidirectional mixer is communicated with the high-temperature steam outlet through a steam pipeline; the water jacket is positioned at the lower part of the furnace body; one end of a secondary air inlet of the air distribution mechanism is communicated with an annular air duct in the water jacket, and the other end of the secondary air inlet is communicated with the gasification air header through a secondary air header; the annular air duct is communicated with the inner cavity of the furnace body; the furnace wall in the middle of the furnace body is provided with an inner lug which is fixed with the carbonization barrel; the carbonization cylinder is a cylinder with the top and the bottom both open; the cavity formed by the top surface of the inner lug, the top surface of the dry distillation cylinder, the inner surface of the top cover and the inner surface of the furnace wall is divided into an upper empty layer and a drying cavity, and the upper empty layer is positioned at the upper part of the drying cavity; a carbonization gas outlet is arranged at the upper part of the upper empty layer; the inner cavity of the carbonization barrel is a carbonization cavity; the cavity formed by the bottom surface of the inner lug, the inner surface of the furnace body, the outer surface of the carbonization barrel and the top surface of the ash tray is divided into a lower empty layer, a reduction cavity, an oxidation cavity and an ash cavity which are arranged from top to bottom; a reducing gas outlet is arranged at the upper part of the lower empty layer; the drying cavity is provided with a plurality of drying steam nozzles, and the drying steam nozzles are communicated with the high-temperature steam inlet through a steam pipeline; the carbonization cavity is provided with a plurality of carbonization steam nozzles, and the carbonization steam nozzles are communicated with a high-temperature steam inlet through a steam pipeline; the high-temperature steam coil is arranged in the drying cavity and the carbonization cavity, and is communicated with the high-temperature steam inlet and the high-temperature steam outlet through the steam pipeline, and the high-temperature steam inlet is communicated with high-temperature superheated steam equipment arranged outside the furnace body through the steam pipeline.
2. A solid waste gasification system according to claim 1 wherein: the high-temperature superheated steam equipment, the high-temperature steam coil pipe, the drying steam nozzle, the carbonization steam nozzle, the unidirectional mixer and the steam pipeline form a high-temperature superheated steam enhanced reaction system.
3. A solid waste gasification system according to claim 1 wherein: the high-temperature superheated steam equipment adopts a gas boiler, a waste heat boiler or a heat exchanger; the air distribution mechanism adopts a grate or a hood.
4. A solid waste gasification system according to claim 1 wherein: the slag discharging mechanism comprises an ash discharging transmission mechanism and an ash tray driven by the ash discharging transmission mechanism; the ash discharging transmission mechanism adopts hydraulic transmission, worm and gear transmission or gear transmission; the ash tray consists of a small ash knife for assisting ash discharge and a large ash knife for directly discharging ash.
5. A solid waste gasification system according to claim 1 wherein: the sealing feeding mechanism is a bell jar feeder, a hydraulic pushing mechanism, an air lock or a screw conveyor.
6. A solid waste gasification system according to claim 1 wherein: the unidirectional mixer consists of a unidirectional valve and a mixer; the one-way valve is arranged at the outlet of the fan; the mixed steam inlet of the unidirectional mixer is provided with a control valve.
7. A solid waste gasification system according to claim 1 wherein: the upper part and the lower part of the water jacket are respectively provided with a steam rising pipe interface and a descending pipe interface; the descending pipe joint is communicated with the steam collector through a water pipeline; the steam rising pipe joint is communicated with the steam collector through a steam pipeline; the steam collector is communicated with high-temperature superheated steam equipment through a steam pipeline; the water replenishing of the steam collector is softened water; the temperature of the high-temperature superheated steam is 500-1000 ℃ and the pressure is 0-294 KPa.
8. The gasification method of a solid waste gasification system according to claim 7, wherein: solid waste is sent into a furnace body through a sealed feeding mechanism, and a drying layer, a carbonization layer, a reduction layer, an oxidation layer and a ash slag layer are formed in the furnace body, and the concrete process is as follows:
the solid waste is sent into the furnace body through a sealed feeding mechanism, air required by gasification is mixed with steam fed by a mixed steam inlet in a unidirectional mixer arranged on an outlet pipeline of the gasification fan to form gasification wind, the gasification wind is sent into a gasification wind main pipe, and then the gasification wind is divided into two paths to be sent into the furnace body, wherein one path reaches a wind distribution mechanism positioned at the bottom of the furnace body through a primary wind inlet, and the other path reaches an annular wind channel positioned in a water jacket through a secondary wind inlet and then enters the side part of the furnace body; the gasified wind absorbs sensible heat of the ash slag layer and then heats up, and the semicoke formed by the oxidation layer and the reduction layer has exothermic reaction; the heavy metals in the solid waste are sintered and solidified after the reaction, ash becomes slag and moves downwards to an ash layer, and the gas generated after the reaction comprises carbon monoxide, carbon dioxide and water vapor; the slag is driven by the power of the slag discharging mechanism to rotate and move downwards while being cooled, the slag is rubbed with the inner surface of the furnace skirt below the furnace body, the massive slag is crushed, and the crushed and cooled slag is discharged out of the furnace body by the slag discharging mechanism; the gas generated by the oxidation layer rises to the reduction layer, the water vapor reacts with solid waste after carbonization, and the solid comprises semicoke in substances generated after the reaction, and the reduction gas comprises carbon monoxide, carbon dioxide, hydrogen and methane; part of the reducing gas rises to the lower empty layer, and part of the dust carried by the reducing gas is settled and discharged from the reducing gas outlet; the other part rises to the dry distillation layer and the dry layer; the softened water is conveyed into a steam collector under pressure through a water pipeline, flows to a descending pipe joint through the water pipeline and flows into a water jacket, the softened water in the water jacket is heated into a steam-water mixture by heat transmitted by a furnace body, is discharged through a steam ascending pipe joint, and rises along the steam pipeline to reach the steam collector for steam-water separation, so that a water jacket and steam-water natural circulation system of the steam collector is formed; saturated steam is discharged out of the steam collector, reaches high-temperature superheated steam equipment through a steam pipeline, is heated into high-temperature superheated steam, and enters a high-temperature steam inlet through the steam pipeline; the steam at the high-temperature steam inlet is sent into the furnace body in three ways through a steam pipeline, wherein one way passes through the high-temperature steam coil pipe, and after heating the drying layer and the dry distillation layer, the steam is discharged from the high-temperature steam outlet and is communicated with the mixed steam inlet through the steam pipeline; the other path of the waste solid is sprayed into the drying layer through a drying steam nozzle through a steam pipeline, the temperature of the solid waste containing the moisture is raised, the solid waste is dehydrated, namely, the drying reaction is carried out, and part of the solid waste is subjected to the carbonization reaction, the drying tail gas after the drying reaction comprises steam, methane, carbon dioxide and nitrogen, and the solid waste after the drying reaction leaves the drying layer and moves to the carbonization layer; the third path is sprayed into the carbonization layer through a steam pipeline through a carbonization steam nozzle, and a carbonization reaction is carried out on the solid waste dried by the drying layer, the gas after the carbonization reaction comprises carbon monoxide, carbon dioxide, gaseous hydrocarbon and tar, and the solid waste after the carbonization reaction leaves the carbonization layer and moves to the reduction layer; the dry distillation gas generated by the dry distillation layer and the dry tail gas generated by the dry layer rise to the upper empty layer, and part of dust carried by the dry distillation layer is settled and discharged from a dry distillation gas outlet.
9. The gasification method of a solid waste gasification system according to claim 8, wherein: the discharge temperature of the dry distillation gas outlet is 100-300 ℃ and the pressure is 100-4000 Pa; the discharge temperature of the reducing gas outlet is 300-600 ℃ and the pressure is 500-5000 Pa.
10. The gasification method of a solid waste gasification system according to claim 8, wherein: the temperature range of the drying layer is 100-300 ℃, the temperature range of the dry distillation layer is 300-650 ℃, the temperature range of the reduction layer is 550-1000 ℃, the temperature range of the oxidation layer is 1000-1200 ℃, and the temperature range of the ash layer is 100-1000 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711104502.9A CN107723030B (en) | 2017-11-10 | 2017-11-10 | Solid waste gasification system and gasification method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711104502.9A CN107723030B (en) | 2017-11-10 | 2017-11-10 | Solid waste gasification system and gasification method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107723030A CN107723030A (en) | 2018-02-23 |
| CN107723030B true CN107723030B (en) | 2024-03-29 |
Family
ID=61214374
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711104502.9A Active CN107723030B (en) | 2017-11-10 | 2017-11-10 | Solid waste gasification system and gasification method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107723030B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109679696A (en) * | 2018-12-16 | 2019-04-26 | 陈曙平 | Rubbish distillation gas furnace |
| CN110846082A (en) * | 2019-12-09 | 2020-02-28 | 中城绿建科技有限公司 | System for preparing high-calorific-value gas by pyrolysis and gasification |
| CN111171874B (en) * | 2020-03-05 | 2021-07-09 | 梵境新能源科技(浙江)有限公司 | Process for preparing synthetic gas or fuel gas by moving bed pure oxygen continuous gasification furnace for cow dung raw material |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20020019359A (en) * | 2000-09-05 | 2002-03-12 | 유용진 | Combustible waste equipment thereof |
| CN102746903A (en) * | 2012-07-13 | 2012-10-24 | 余式正 | Large-scale domestic garbage dry distillation and gasification furnace without exhaust gas or dioxin emission |
| CN103555373A (en) * | 2013-07-31 | 2014-02-05 | 余式正 | Garbage dry distillation-gasification furnace with no dioxin and waste gas emission |
| CN105542805A (en) * | 2015-12-15 | 2016-05-04 | 广西高远环境工程有限公司 | Vertical-horizontal type gas making apparatus and process with integrated three segments containing destructive distillation, gasification and decomposition for household refuse |
| CN207483679U (en) * | 2017-11-10 | 2018-06-12 | 马加德 | A kind of solid waste gasification system |
-
2017
- 2017-11-10 CN CN201711104502.9A patent/CN107723030B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20020019359A (en) * | 2000-09-05 | 2002-03-12 | 유용진 | Combustible waste equipment thereof |
| CN102746903A (en) * | 2012-07-13 | 2012-10-24 | 余式正 | Large-scale domestic garbage dry distillation and gasification furnace without exhaust gas or dioxin emission |
| CN103555373A (en) * | 2013-07-31 | 2014-02-05 | 余式正 | Garbage dry distillation-gasification furnace with no dioxin and waste gas emission |
| CN105542805A (en) * | 2015-12-15 | 2016-05-04 | 广西高远环境工程有限公司 | Vertical-horizontal type gas making apparatus and process with integrated three segments containing destructive distillation, gasification and decomposition for household refuse |
| CN207483679U (en) * | 2017-11-10 | 2018-06-12 | 马加德 | A kind of solid waste gasification system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107723030A (en) | 2018-02-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102322630B (en) | Method and devices for burning macromolecular matters efficiently and cleanly | |
| CN108300516B (en) | Process system for cooperatively treating household garbage by utilizing plasma gasification furnace in coal-fired power plant | |
| CN203791331U (en) | System for synergistic treatment of municipal domestic waste in cement kiln | |
| CN110527560A (en) | A kind of organic solid waste cleaning disposal of resources method | |
| CN101705114B (en) | Method for preparing combustible gas by using rotary kiln to melt and gasify household garbage | |
| CN103934254B (en) | A kind of system and method for cement kiln associated treatment domestic waste | |
| CN109469903B (en) | Incineration treatment method for industrial solid waste | |
| JP4377824B2 (en) | Waste melting treatment method using biomass | |
| CN108176703B (en) | Harmless treatment method and system for multi-element waste | |
| CN104211274A (en) | Sludge reduction and recycling treatment device and sludge treatment method | |
| CN102145343B (en) | Integrated garbage treatment and utilization method for effectively controlling dioxin | |
| WO2011113298A1 (en) | Gasification-liquefaction disposal method, system and equipment for household garbage | |
| CN107723030B (en) | Solid waste gasification system and gasification method thereof | |
| CN205413887U (en) | Medical waste jointly deals with system | |
| CN108443889B (en) | Waste metal catalyst and organic sludge co-treatment device and method | |
| CN101955804A (en) | Solid biomass gasification system and process thereof | |
| CN104211271B (en) | A kind of two-period form mud gasification processing method and treating apparatus | |
| CN202224433U (en) | Refuse treatment system unit capable of effectively restraining dioxin | |
| CN106765142B (en) | Solid waste grading gasification system | |
| CN102746902B (en) | Gasification method of organic wastes and special gasification furnace | |
| CN210267234U (en) | Solid waste gasification melting incineration system based on double molten pools | |
| CN105820845A (en) | Technology for preparing gas through staged quick pyrolysis and gasification of large municipal solid waste | |
| CN203065417U (en) | Three-section authigenic flow guide groove type continuous pyrolysis gasification furnace for bulk rubbish combustible material | |
| RU2570331C1 (en) | Method for processing solid household and industrial wastes and device for thereof realisation | |
| CN114806614B (en) | Rotary kiln pyrolysis carbonization device and process based on smoke injection recycling |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |