CN106833690A - A kind of moving bed solid waste segmented pyrolytic gasification technique and its system - Google Patents
A kind of moving bed solid waste segmented pyrolytic gasification technique and its system Download PDFInfo
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- CN106833690A CN106833690A CN201710000780.3A CN201710000780A CN106833690A CN 106833690 A CN106833690 A CN 106833690A CN 201710000780 A CN201710000780 A CN 201710000780A CN 106833690 A CN106833690 A CN 106833690A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
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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
Abstract
The invention discloses a kind of moving bed solid waste segmented pyrolytic gasification technique and system, existing solid waste pyrolytic gasification technical matters system complex is solved, fault rate is high, efficiency is low, high energy consumption, the feature of environmental protection are poor, investment and operating cost problem high.Technical scheme is comprised the following steps：(1) feed solid waste into pyrolysis system and be pyrolyzed and obtain pyrolysis gas and pyrolysis residue；(2) the pyrolysis gas feeding organic matter gasification decomposing system heats up gasification decomposition removing tar He obtaining synthesis gas after the larger molecular organicses such as bioxin, then recovered heat, cleaning dust depickling；(3) pyrolysis residue is obtained after cooling sorting flammable breeze and residual residue.Present system is simple, process, and easy to operate, energy conversion efficiency is high, recycling effect is good, energy-saving, and investment and operating cost are low, environmentally friendly.
Description
Technical field
The present invention relates to a kind of Solid Waste Treatment technique and system, specifically a kind of moving bed solid waste segmentation
Formula pyrolytic gasification technique and system.
Background technology
Currently master is processed for solid waste (municipal refuse, industrial refuse, clinical waste, other poisonous and harmful wastes etc.)
There are three kinds of modes, i.e. sanitary landfills, compost and burning electricity generation, the treatment principle that it is followed is innoxious, minimizing and resource
Change, undoubtedly in three kinds of processing modes, burning electricity generation mode has than more prominent advantage, can not only reduce occupation of land, realizes
Generated electricity while solid waste minimizing, created certain economic benefit, but burning mode also brings some problems：①
Because incineration temperature is not high, the carcinogens such as bioxin and furans are easily produced；2. it is rich in the flying dust and residue that burn generation
Poisonous and harmful heavy metallic material, easily causes underground water source pollution；3. burn and produce a large amount of flue gases, carbon emission amount is big；Additionally, by
Happened occasionally in the Mass disturbance caused by " neighbour keeps away effect " that planning construction burning electricity generation factory brings.Therefore, research and develop
Go out a kind of environmental protection new technology for Solid Waste Treatment, reduce and eliminate the environment caused in its processing procedure as far as possible
Pollution problem, it has also become one new research topic of current solid waste process field.
Solid waste gasification technology and pyrolytic technique are a kind of Solid Waste Treatment new technologies for growing up in recent years.With
Plasma gasification technology and heat sorting gasification technology be representative solid waste gasification technology by nearly 30 years research and
Development, achieves certain achievement, and current both technologies have been carried out application and popularization to a certain extent abroad, but
Not extensively, it is primarily present following Railway Project：1. gasification reaction temperature is high, for ensureing solid waste in all components send out
Raw melting and gasification, cause energy consumption higher；2. process system is complex, and plasma gasification technology needs special plasma
Torch system, and heat sorting gasification technology is also required to special fuel gas accessory system；3. because reaction temperature is high, system operatio compared with
It is complexity, reliability is poor, and operation and maintenance cost is higher；4. because vapor pressure is pressure-fired, disposal ability is generally relatively low,
Industrial applications list stove maximum capacity is 360t/d at present；5. invest higher, project economics is poor.And current existing solid
Waste pyrolysis technology is still not mature enough, and also there are problems needs to research and solve, therefore rarely seen related industrial applications report
Road.By consulting existing retrospect analysis from documents, CN2447644Y discloses that " a kind of vertical converter type domestic garbage pyrolysis gasification is burnt
Burn stove ", have that operating condition is unstable, fault rate is higher, the shortcomings of incomplete combustion；CN2811769Y discloses " a kind of solid
Body waste pyrolysis incinerator ", uses the mode of fire grate pyrolytic incineration plus dual firing chamber, is more focused on burning；
CN204388069U discloses " a kind of solid waste pyrolysis formula fusion and gasification processing unit ", uses reciprocal grate furnace structure
Melting incinerating mode, while be furnished with exhaust gas conversion device, be also the substep pyrolytic incineration for laying particular emphasis on solid waste；
CN202203950U discloses " a kind of organic solid waste pyrolysis gasifying device ", mainly uses the revolution with heat carrier
Kiln pyrolysis oven and fluidized bed combustion chamber, process system are complicated, and fault rate is high；CN104910930A discloses " organic solid waste
Pyrolysis treatment device, system and method ", uses the horizontal rotary furnace of similar rotary structure, main with multiple tube-in-tube structures
If carrying out low temperature pyrogenation to organic solid waste, gas, liquid, solid three-phase product is obtained, but without the separation for three-phase product
Purification technique carries out innovation and creation, and process system is complicated, and exploitativeness is not high.Understand that current consolidates by further analysis
Body waste pyrolysis technology due to the gas phase and liquid product for the treatment of pyrolysis cannot be efficiently separated, often using dual firing chamber's structure by heat
Solution outlet of still gas-liquid two-phase product one has burnt it, reduces the efficiency of energy utilization of pyrolysis.
The content of the invention
The invention aims to solve above-mentioned technical problem, there is provided a kind of process is simple, easy to operate, energy conversion effect
Rate is high, recycling effect is good, energy-saving, environment amenable moving bed solid waste segmented pyrolytic gasification technique.
The present invention also provides a kind of system for above-mentioned technique, with simple system, low energy consumption, equipment investment and operation
Low cost, achievable continuous production, the advantage of labour intensity reduction.
Moving bed solid waste segmented pyrolytic gasification technique of the present invention, comprises the following steps：(1) feed solid waste into
Pyrolysis system be pyrolyzed and obtains pyrolysis gas and pyrolysis residue；(2) the pyrolysis gas feeding organic matter gasification decomposing system heats up
Removing tar is decomposed in gasification He obtaining synthesis gas after the larger molecular organicses such as bioxin, then recovered heat, washing depickling；(3)
Flammable breeze and residual residue that the pyrolysis residue is obtained after cooling sorting.
In the step (1), the pyrolysis system includes lock hopper, pyrolysis oven and the hot-blast stove for pyrolysis oven heat supply, institute
Pyrolysis oven is stated for moving bed pyrolysis stove, with vertical type cylinder shape tube-in-tube structure, by the pyrolysis section and the cooling section group of hypomere of epimere
Into solid waste sends into pyrolysis oven, 550~650 DEG C of pyrolysis temperature in control pyrolysis oven, operating pressure control in stove through lock hopper
In -3kPaG~-0.1kPaG, solid waste residence time in pyrolysis section is 10~90mim, and the pyrolysis drawn off through cooling section is residual
Slag is cooled to 250~350 DEG C.
In the step (1), the pyrolysis section is provided with heat exchange jacket, and cooling section also is provided with cooling jacket, the heat exchange folder
Heat exchange fin is equipped with set and cooling jacket；The high-temperature flue gas feeding heat exchange jacket of the hot-blast stove, goes out the cigarette of heat exchange jacket
Hot-blast stove temperature adjustment is sent into gas part as temperature adjustment flue gas, and remainder goes UTILIZATION OF VESIDUAL HEAT IN to unite, controls out the high-temperature flue gas of hot-blast stove
Temperature is 800~1000 DEG C.
In the step (1), air is re-fed into hot-blast stove as combustion air, institute after being introduced into the cooling jacket preheating
Air is stated preferentially using the foul smell from solid waste storage hole.
The organic matter gasification decomposing system includes that organic matter decomposition gasification device and pyrolysis gas are detained surge tank, the pyrolysis
Gas is first heated to 1050~1100 DEG C through organic matter decomposition gasification device, is then fed into pyrolysis gas delay surge tank and fully decomposes
The tar carried in pyrolysis gas is He the larger molecular organicses such as bioxin, control pyrolysis gas are in the pyrolysis gas delay surge tank residence time
In 10~20s, go out pyrolysis gas and be detained the synthesis gas temperature of surge tank at 1000~1050 DEG C.
In the step (2), the organic matter decomposition gasification device is cyclone separator structure, and the pyrolysis gas are from organic matter
Decomposition gasification device middle part enters rear screw and rises, and the intensification that reacted in the presence of burner noz(zle), makes to be carried in pyrolysis gas
Tar He the larger molecular organicses such as bioxin carry out gasification decomposition, and the lime-ash carried in pyrolysis gas is then from organic matter decomposition gas
Change the discharge of device outlet at bottom.
In the step (2), it is described go out pyrolysis gas be detained surge tank synthesis gas through heat recovery system reclaim heat drop
Temperature is further reduced to 30~50 DEG C to 180~250 DEG C, then by temperature after the washing depickling of synthesis gas washing dedusting deacidification system,
Feeding downstream purification procedure is drawn by synthesis gas air-introduced machine again further to process.
In the step (3), the lime-ash one that the pyrolysis residue and organic matter gasification decomposing system are produced is at first through pyrolysis
Residue cooler is cooled to 40~90 DEG C, is re-fed into pyrolysis residue separation system and sort to obtain flammable breeze and residue is residual
Slag, synthesis gas or use it that the flammable breeze feeding hot-blast stove is obtained as fuel combustion, insufficient section introducing step (2)
He supplies external fuel.
The present invention is used for the moving bed solid waste segmented pyrolysis gasification system of above-mentioned technique, including the heat being sequentially connected
Solution system, organic matter gasification decomposing system, heat recovery system, synthesis gas washing dedusting deacidification system, the pyrolysis system bag
Include lock hopper, pyrolysis oven and the hot-blast stove for pyrolysis oven heat supply；The pyrolysis gas outlet of the pyrolysis oven epimere gasifies with organic matter
Decomposing system is connected, and the outlet at bottom of the pyrolysis oven is through pyrolysis residue cooler, pyrolysis residue separation system and hot-blast stove
Fuel inlet is connected.
The pyrolysis oven is moving bed pyrolysis stove, with vertical type cylinder shape tube-in-tube structure, by the pyrolysis section and hypomere of epimere
Cooling section composition, the pyrolysis section is provided with heat exchange jacket, and cooling section is provided with cooling jacket, the heat exchange jacket and cooling jacket
In be equipped with heat exchange fin.
The exhanst gas outlet of the hot-blast stove is connected with the gas approach of heat exchange jacket, the exhanst gas outlet of the heat exchange jacket with
Hot-blast stove temperature adjustment gas approach connection, the synthesis gas washing dedusting deacidification system outlet also with the fuel inlet of hot-blast stove
Connection.
The cooling jacket has air intlet and air outlet slit, and the air intlet is connected with air blower outlet, empty
Gas outlet is connected with the air intlet of hot-blast stove.
The organic matter decomposition gasification utensil has the structure of similar cyclone separator, and top is provided with 1-3 burner noz(zle), institute
The centre inlet for stating organic matter decomposition gasification device is connected with pyrolysis oven, and top exit is detained surge tank and is connected with pyrolysis gas, bottom
Outlet is connected with the pyrolysis residue cooler.
The outlet at bottom of organic matter decomposition gasification device is connected with the pyrolysis residue cooler described in pyrolysis oven.
Connecting pipe between the pyrolysis oven and organic matter decomposition gasification device has upward inclination angle, and angle is controlled 30
~60 °.
For problem present in background technology, inventor makes following improvement：
Organic matter gasification decomposing system is set, the macromoleculars such as the tar and bioxin of carrying in pyrolysis gas is fully decomposed organic
Thing.Because solid waste typically all carries a certain amount of bioxin in itself, while general (this below 850 DEG C of pyrolysis temperature
It is middle warm solution to invent, and pyrolysis temperature is at 550~650 DEG C), it is unavoidable in pyrolytic process to have bioxin generation, while middle warm
Solution can also produce the larger molecular organicses such as tar, and the type organic decomposition temperature is general all more than 900 DEG C, while needs give
Enough residence times could be decomposed completely, and wherein bioxin is needed more than 850 DEG C, more than residence time 2s, could completely
Destruction and decomposition, and tar need to be more than 1000 DEG C, residence time 10s, could decompose completely.Machine thing gasification decomposing system includes
Organic matter decomposition gasification device and pyrolysis gas are detained surge tank, by setting organic matter decomposition gasification device, lead to ground fuel nozzle and spray into
Fuel and combustion oxygen burning make pyrolysis gas heating by ignition, for tar He the decomposition of bioxin provides reaction temperature, then pass through
Pyrolysis gas are detained surge tank and ensure that the pyrolysis gas after heating up have enough residence times, so as to ensure tar He bioxin is abundant
Decompose, while under the vapor effect carried in pyrolysis gas, there is water-gas gasification reaction, generate the conjunction based on H2 and CO
Into gas, so as to further improve the yield of synthesis gas, it is also possible to effectively avoid conventional pyrolysis technology due to containing tar in pyrolysis gas
Caused by follow-up equipment and pipe-line system blockage problem, also without tar, naphthalene, phenol etc. in the waste water of follow-up synthesis gas washing
Pollutant, can reduce subsequent wastewater treatment difficulty, and waste water treatment is simple, it is easy to qualified discharge.
The organic matter decomposition gasification device is sprayed into for fuel gas and (avoids using the unclear table such as a small amount of, appropriate as far as possible
State mode) purity oxygen, pyrolysis gas temperature is controlled by controlling oxygen straying quatity at 1050~1000 DEG C, by controlling pyrolysis gas
It is detained the surge tank residence time in 10~20s in pyrolysis gas, controls out pyrolysis gas to be detained the synthesis gas temperature of surge tank 1000
~1050 DEG C, so as to ensure that card tar and bioxin are decomposed and gasified completely；The oxygen volumetric concentration is preferably controlled in >=
95%.
After the synthesis gas is detained buffering pot bottom discharge from pyrolysis gas, heat recovery system is entered into, reclaim synthesis gas
Middle most of high temperature sensible heat, and after byproduct steam, then deliver to synthesis gas washing dedusting deacidification system, is washed, is cooled down, dedusting
And depickling, it is drawn to the further purified treatment of lower procedure finally by synthesis gas air-introduced machine, the synthesis gas for obtaining can also part
Loopback hot-blast stove is used as the fuel for burning；The synthesis gas washing dedusting deacidification system can as needed fill into alkali lye, for taking off
Except sour gas such as HCl, HF.
The lime-ash that pyrolysis residue and organic matter decomposition gasification device bottom to pyrolysis furnace bottom discharge are produced, inventor is no longer
Using simple one burnt or landfill stabilization method, but first pass through pyrolysis residue cooler further cooling after, control into
The residue temperature of pyrolysis residue separation system is at 40~90 DEG C, then delivers to pyrolysis residue separation system and sorted, and sub-elects
Flammable breeze is delivered to hot-blast stove and is used as main fuel burning, and residual residue removes further comprehensive utilization system.By above-mentioned side
On the one hand method greatly increases the total energy approach efficiency of solid waste pyrolytic gasification, on the other hand then further eliminate and
Avoid the generation and diffusion transfer of lime-ash Zhong bioxin.This is the solid waste because pyrolysis temperature is low compared with combustion gasification temperature
After pyrolysis, also quite a few combustible is mixed in lime-ash and can not completely be pyrolyzed and react, by this part unreacted
Combustible sort out, by the high-temp combustion (temperature is up to more than 1000 DEG C) of hot-blast stove, the part can be made full use of
Energy is pyrolysis heat supply, is reclaimed so as to reach Energy Efficient, reduces the problem of pollution and discharge, and insufficient section can introduce production
Synthesis gas is supplied by external fuel, so as to realize the self-sufficient of system capacity.Simultaneously as lime-ash carbon residue is by high temperature
After burning, can further destroy and decompose may wherein carry bioxin, so as to eliminate and avoid lime-ash Zhong bioxin
Produce and diffusion transfer.
Cooling section is provided with pyrolysis oven hypomere, cooling medium can be passed through in the cooling jacket of cooling section, cooled down to entering
The pyrolysis residue of section carries out indirect heat exchange cooling, and the cooling medium can be cooling water or air, preferably will be into hot-blast stove
Combustion air as cooling medium introduce cooling section cooling folder in as cooling medium cool down pyrolysis residue, combustion air warp
Deliver to hot-blast stove after crossing preheating, can further reducing energy consumption, the tapping temperature of pyrolysis residue can be reduced again.Preferably, this is helped
The foul smell that combustion air is preferably extracted out using solid waste storage hole, the foul smell by after hot-blast stove high-temp combustion, it is possible to prevente effectively from
The diffusion of stench, it is environmentally friendly；The warm flue gas high of the hot-blast stove output are first and go out the middle temperature flue gas of heat exchange jacket in heat
After carrying out mixing temperature adjustment in wind furnace, then pyrolysis oven pyrolysis section is delivered to as pyrolysis thermal source.
The pyrolysis oven and organic matter decomposition gasification device intermediate connection tube road should be as far as possible short, and its angle control that is inclined upwardly
At 30~60 °, when being easy to fluctuation of operating conditions, further heat can be smoothly back in pyrolysis oven after the condensation of the larger molecular organicses such as tar
Solution.
Specific beneficial effect of the invention is summarized as follows：
1. solid waste segmented pyrolytic gasification technology is used, and solid waste first passes through pyrolysis and produces pyrolysis gas, pyrolysis gas
The tar that wherein carries is decomposed through organic matter decomposition gasification device He the larger molecular organicses such as bioxin, and removed by alkali cleaning again
The halogens such as HCl, HF, can effectively prevent bioxin from generating again, it is ensured that bioxin is free of in synthesis gas, so as to effectively solve
Incineration technology of having determined easily produces the problem of bioxin.
2. after the segmented formula pyrolytic gasification of solid waste produce lime-ash it is sorted obtain followed with flammable charcoal solid fuel
Ring is used to Combustion of Hot Air Furnace, and for pyrolysis oven provides heat, not only greatly increases the energy of solid waste pyrolytic gasification
Comprehensive utilization ratio, resource recycling utilization ratio is high, further eliminates and avoid the generation and diffusion of lime-ash Zhong bioxin
Transfer.
3. by set machine thing decomposition gasification device and pyrolysis gas be detained surge tank fully decompose the tar carried in pyrolysis gas,
The organic matters such as naphthalene, phenol, it is possible to prevente effectively from conventional pyrolysis technology due in pyrolysis gas containing follow-up equipment and pipe caused by tar
The blockage problem of road system, simultaneously because without pollutants such as tar, naphthalene, phenol in waste water, subsequent wastewater treatment can be reduced difficult
Degree, waste water treatment is simple, it is easy to qualified discharge.
4. the synthesis gas for being produced after the segmented formula pyrolytic gasification of solid waste, can not only be further utilized to combustion power generation,
Can also be used to the chemical products such as production natural gas, methyl alcohol, synthesis ammoniuria element, the products scheme of recycling is numerous, and work
Skill is simple, and resource effect is good, it is easy to popularization and application.
5. Combustion of Hot Air Furnace lime-ash is coordinated using moving bed pyrolysis technology, by selecting suitable feed system, charging can
Do not limited by solid waste size, it is easy to accomplish fed while different size solid waste, adaptability to raw material is wider.
6. the foul smell that the combustion air of hot-blast stove can be extracted out using solid waste storage hole, it is possible to prevente effectively from the expansion of stench
Dissipate.
7. pyrolysis oven of the present invention and organic matter decomposition gasification device simple structure, without support or drive disk assembly in stove, safeguard
Amount is few, and operating cost is low, can effectively ensure that the long-term operation of equipment.
8. the nominal capacity of separate unit pyrolysis oven treatment solid waste is 50~500t/d, is not only suitable for extensive solid waste
Focus on, the sweetly disposition of small-scale solid waste is adapted to again, have a wide range of application.
9. simple system, compact conformation, efficiency is high, and investment and operating cost are low, safe and reliable, energy-saving, to ring
Border is friendly, can simultaneously process the solid waste such as house refuse, organic sludge, realizes partial solid waste joint disposal, produces
Clean fuel, can be widely popularized as distributed busbar protection in county town, small towns, rural area and industry park, have a extensive future.
Brief description of the drawings
Fig. 1 is the inventive method process chart and system diagram；
Wherein：1-lock hopper；2-pyrolysis oven, 2.1-pyrolysis section, 2.11- heat exchange jackets, 2.2-cooling section, 2.21- is cold
But chuck, 2.3-heat exchange fin；3-organic matter decomposition gasification device, 3.1- burner noz(zle)s；4-pyrolysis gas are detained surge tank；5—
Heat recovery system；6-synthesis gas washing dedusting deacidification system；7-synthesis gas air-introduced machine；8-pyrolysis residue cooler；9—
Pyrolysis residue separation system；10-hot-blast stove；11-air blower；12-flue gas blower fan.
Specific embodiment
Explanation is further explained to present system below in conjunction with the accompanying drawings
Reference picture 1, the present invention includes pyrolysis system, organic matter gasification decomposing system, heat recovery system 5 and synthesis air purge
Dirt deacidification system is washed away, the pyrolysis system includes lock hopper 1, pyrolysis oven 2 and the hot-blast stove 10 for the heat supply of pyrolysis oven 2；It is described
Organic matter gasification decomposing system includes that organic matter decomposition gasification device 3 and pyrolysis gas are detained surge tank 4.The lock hopper 1 and pyrolysis oven 2
Material inlet connection, the pyrolysis gas outlet of the epimere of the pyrolysis oven 2 is detained through organic matter decomposition gasification device 3, pyrolysis gas and buffers
Tank 4, heat recovery system 5, synthesis gas washing dedusting deacidification system 6 and synthesis gas air-introduced machine 7 are connected, the bottom of the pyrolysis oven 1
Portion's outlet is connected through pyrolysis residue cooler 8, pyrolysis residue separation system 9 with the fuel inlet of hot-blast stove 10.
The pyrolysis oven 2 is moving bed pyrolysis stove, with vertical type cylinder shape tube-in-tube structure, by the He of pyrolysis section 2.1 of epimere
The cooling section 2.2 of hypomere is constituted, and the pyrolysis section 2.1 is provided with heat exchange jacket 2.11, and cooling section 2.2 is provided with cooling jacket 2.21,
Heat exchange fin 2.3 is equipped with the heat exchange jacket 2.11 and cooling jacket 2.21.The pyrolysis oven 2 and organic matter decomposition gasification
Connecting pipe between device 3 has upward inclination angle a, and angle is controlled at 30~60 °.
The exhanst gas outlet of the hot-blast stove 10 is connected with the gas approach of heat exchange jacket 2.11, the heat exchange jacket 2.11
Exhanst gas outlet is connected through flue gas blower fan 12 with the temperature adjustment gas approach of hot-blast stove 10.
The cooling jacket 2.21 has air intlet and air outlet slit, and the air intlet is exported with air blower 11 and connected
Connect, air outlet slit is connected with the air intlet of hot-blast stove 10.
The organic matter decomposition gasification utensil has the structure of similar cyclone separator, and top is provided with 1-3 burner noz(zle), institute
The centre inlet for stating organic matter decomposition gasification device is connected with pyrolysis oven, and top exit is detained surge tank and is connected with pyrolysis gas, bottom
Outlet is connected with the pyrolysis residue cooler.
Technical process and method：
Referring to Fig. 1, after raw material solid waste is crushed into 5~150mm particle diameters, lock hopper 1 is delivered to by feed arrangement, then by
Material inlet is sent in pyrolysis oven 2 and is pyrolyzed, 550~650 DEG C of pyrolysis temperature in control pyrolysis oven 2, and solid waste is in warm
10~90mim of residence time in solution section 2.1, heat exchange jacket 2.11 is passed through the high-temperature flue gas from hot-blast stove 10 for pyrolysis section
2.1 provide heat, are pyrolyzed solid waste and produce pyrolysis gas and pyrolysis residue, control out the pyrolysis gas temperature of pyrolysis oven 2 300
~350 DEG C, pyrolysis gas deliver to organic matter decomposition gasification device 3 by the pyrolysis gas outlet of pyrolysis oven 2, and further gasification heats up, described
Pyrolysis gas enter rear screw and rise from the middle part of organic matter decomposition gasification device 3, and fuel and oxygen are controlled by the burner noz(zle) 3.1 on top
Gas (oxygen volumetric concentration control >=95%) straying quatity controls pyrolysis gas temperature to be increased to 1050~1100 DEG C, makes pyrolysis gas
The tar of middle carrying is He the larger molecular organicses such as bioxin carry out gasification decomposition, and the lime-ash carried in pyrolysis gas is then from organic matter
The outlet at bottom of decomposition gasification device 3 is discharged pyrolysis gas and is sent directly into the pyrolysis gas delay fully decomposition pyrolysis of surge tank 4 through top exit
The tar carried in gas is He the larger molecular organicses such as bioxin, control pyrolysis gas to exist in the pyrolysis gas delay residence time of surge tank 4
10~20s, goes out pyrolysis gas and is detained the synthesis gas temperature of surge tank 4 at 1000~1050 DEG C, so that the tar in ensureing synthesis gas
Decompose completely and gasify with the larger molecular organicses such as bioxin, then most of heat in synthesis gas is reclaimed by heat recovery system 5
After amount byproduct steam, synthesis gas temperature is down to 180~250 DEG C, then by synthesis gas washing dedusting deacidification system 6 wash overflow, dedusting,
After depickling, synthesis gas temperature is further reduced to 30~50 DEG C, is finally drawn to downstream purification procedure by synthesis gas air-introduced machine 7 and enters one
Step treatment.Wherein, synthesis gas washing dedusting deacidification system 6 adds appropriate alkaline liquor as needed, for removing the acidity such as HCl, HF
Gas；Synthesis gas air-introduced machine 7 is used to be drawn synthesis gas, and controls pyrolysis oven 2 to be operated under tiny structure, operating pressure control in stove
In -3kPaG~-0.1kPaG, while air-introduced machine exiting syngas Stress control is in 3kPaG~10kPaG.
The pyrolysis residue that pyrolysis oven 2 is produced first is dropped into the cooling section 2.2 and cooling jacket 2.21 of pyrolysis oven bottom
Air indirect heat exchange is precooled, and pyrolysis residue is cooled into 250~350 DEG C, then from the discharge of the outlet at bottom of pyrolysis oven 2, control
Residence time of the solid waste processed in pyrolysis oven 2 is 10~90mim.The pyrolysis residue and organic that the bottom of pyrolysis oven 2 is discharged
The lime-ash of the outlet at bottom of thing decomposition gasification device 3 discharge is cooled down by pyrolysis residue cooler 8 together, the heat after control cooling
Solution residue temperature enters back into pyrolysis residue separation system 9 and is sorted at 40~90 DEG C, flammable breeze and residue obtained from
Residue, wherein flammable breeze is sent to the burning of hot-blast stove 10 through fuel inlet obtains warm flue gas high, it is the pyrolysis section of pyrolysis oven 2
2.1 provide heat, and residual residue then goes further operation to be comprehensively utilized.The cooling medium being passed through in cooling jacket 2.21 can
To use air, it would however also be possible to employ cooling water, other fluid media (medium)s, the present embodiment can also be used to be considered as air, especially
It is the foul smell being preferentially drawn out using solid waste storage hole.Air first passes through air blower and is drawn by indirect through cooling jacket 2.21
Cooling pyrolysis residue, while itself is preheated, then delivers to hot-blast stove 10 as combustion air.
The part that the warm flue gas high (control is at 1000~1100 DEG C) of the output of hot-blast stove 10 are first sent with flue gas blower fan 12
Middle temperature flue gas carries out mixing temperature adjustment in hot-blast stove 10, and it is 800~1000 DEG C to control the high-temperature flue-gas come out of the stove, then delivers to heat
Conduct pyrolysis thermal source in the heat exchange jacket 2.11 of the pyrolysis section 2.1 of stove 2 is solved, after making solid waste that pyrolytic reaction to occur, through flue gas wind
Machine 12 is drawn, and is drawn from heat exchange jacket 2.11, and outlet temperature is controlled at 350~400 DEG C.Go out the middle temperature flue gas of pyrolysis oven 2 except
Part send hot-blast stove 10 to be used as temperature adjustment, and major part is discharged after sending to UTILIZATION OF VESIDUAL HEAT IN and purified treatment.
The synthesis gas obtained through the present invention can fed downstream device be used for combustion power generation or heat supply, chemical products production (my god
Right gas, methyl alcohol, synthesis ammonia etc.), hydrogen manufacturing and preparing liquid fuel etc..
Above-described is only the present invention preferably implementation process, can not limit the right of the present invention with this certainly
Scope.Therefore, the equivalence changes made according to scope of the present invention patent, still fall within protection scope of the present invention.
Claims (15)
1. a kind of moving bed solid waste segmented pyrolytic gasification technique, it is characterised in that comprise the following steps：(1) by solid
Waste feeding pyrolysis system be pyrolyzed and obtains pyrolysis gas and pyrolysis residue；(2) the pyrolysis gas feeding organic matter gasification is decomposed
System heats up gasification decomposition removing tar He being obtained after the larger molecular organicses such as bioxin, then recovered heat, cleaning dust depickling
To synthesis gas；(3) pyrolysis residue is obtained after cooling sorting flammable breeze and residual residue.
2. moving bed solid waste segmented pyrolytic gasification technique as claimed in claim 1, it is characterised in that the step
(1) in, the pyrolysis system includes lock hopper, pyrolysis oven and the hot-blast stove for pyrolysis oven heat supply, and the pyrolysis oven is moving bed
Pyrolysis oven, with vertical type cylinder shape tube-in-tube structure, is made up of the pyrolysis section of epimere and the cooling section of hypomere, and solid waste is through lock hopper
Feeding pyrolysis oven, 550~650 DEG C of pyrolysis temperature in control pyrolysis oven, operating pressure is controlled in -3kPaG~-0.1kPaG in stove,
Solid waste residence time in pyrolysis section is 10~90mim, and the pyrolysis residue drawn off through cooling section is cooled to 250~350 DEG C.
3. moving bed solid waste segmented pyrolytic gasification technique as claimed in claim 2, it is characterised in that the step
(1) in, the pyrolysis section is provided with heat exchange jacket, and cooling section also is provided with cooling jacket, in the heat exchange jacket and cooling jacket
It is provided with heat exchange fin；The high-temperature flue gas feeding heat exchange jacket of the hot-blast stove, goes out the flue gas partial of heat exchange jacket as temperature adjustment cigarette
Pneumatic transmission enters hot-blast stove temperature adjustment, and remainder goes UTILIZATION OF VESIDUAL HEAT IN to unite, and the high-temperature flue-gas for controlling out hot-blast stove are 800~1000
℃。
4. moving bed solid waste segmented pyrolytic gasification technique as claimed in claim 3, it is characterised in that the step
(1) in, air is re-fed into hot-blast stove as combustion air after being introduced into the cooling jacket preheating.
5. moving bed solid waste segmented pyrolytic gasification technique as claimed in claim 1, it is characterised in that the step
(2) in, the organic matter gasification decomposing system includes that organic matter decomposition gasification device and pyrolysis gas are detained surge tank, the pyrolysis gas
1050~1100 DEG C first are heated to through organic matter decomposition gasification device, pyrolysis gas are then fed into and are detained the abundant decomposition heat of surge tank
Vent one's spleen middle carrying tar He the larger molecular organicses such as bioxin, control pyrolysis gas are detained the surge tank residence time and exist in pyrolysis gas
10~20s, goes out pyrolysis gas and is detained the synthesis gas temperature of surge tank at 1000~1050 DEG C.
6. moving bed solid waste segmented pyrolytic gasification technique as claimed in claim 5, it is characterised in that the step
(2) in, the organic matter decomposition gasification device is cyclone separator structure, and top is provided with 1-3 burner noz(zle), the pyrolysis gas from
Organic matter decomposition gasification device middle part enters rear screw and rises, and the intensification that reacted in the presence of burner noz(zle), makes pyrolysis gas
The tar of middle carrying is He the larger molecular organicses such as bioxin carry out gasification decomposition, and the lime-ash carried in pyrolysis gas is then from organic matter
Decomposition gasification device outlet at bottom is discharged.
7. the moving bed solid waste segmented pyrolytic gasification technique as described in claim 5 or 6, it is characterised in that the step
Suddenly in (2), it is described go out pyrolysis gas be detained surge tank synthesis gas through heat recovery system reclaim heat be cooled to 180~250 DEG C,
30~50 DEG C are further reduced to by temperature after the washing depickling of synthesis gas washing dedusting deacidification system again, then by synthesis gas air inducing
Machine is drawn feeding downstream purification procedure and further processes.
8. moving bed solid waste segmented pyrolytic gasification technique as claimed in claim 1, it is characterised in that the step
(3) in, the pyrolysis residue and the isolated lime-ash one of organic matter gasification decomposing system are at first cold through pyrolysis residue cooler
But to 40~90 DEG C, it is re-fed into pyrolysis residue separation system and sort to obtain flammable breeze and residual residue, the flammable charcoal
Synthesis gas or mended using other external fuels that slag feeding hot-blast stove is obtained as fuel combustion, insufficient section introducing step (2)
Foot.
9. a kind of moving bed solid waste segmented pyrolysis gasification system, it is characterised in that including be sequentially connected pyrolysis system,
Organic matter gasification decomposing system, heat recovery system, synthesis gas washing dedusting deacidification system, the pyrolysis system include lock hopper,
Pyrolysis oven and the hot-blast stove for pyrolysis oven heat supply；The pyrolysis gas outlet of the pyrolysis oven epimere and organic matter gasification resolving system
System connection, the outlet at bottom of the pyrolysis oven enters through the fuel of pyrolysis residue cooler, pyrolysis residue separation system and hot-blast stove
Mouth connection.
10. moving bed solid waste segmented pyrolysis gasification system as claimed in claim 9, it is characterised in that the pyrolysis
Stove is moving bed pyrolysis stove, with vertical type cylinder shape tube-in-tube structure, is made up of the pyrolysis section of epimere and the cooling section of hypomere, described
Pyrolysis section is provided with heat exchange jacket, and cooling section is provided with cooling jacket, heat exchange fin is equipped with the heat exchange jacket and cooling jacket.
11. moving bed solid waste segmented pyrolysis gasification systems as claimed in claim 9, it is characterised in that the hot blast
The exhanst gas outlet of stove is connected with the gas approach of heat exchange jacket, the exhanst gas outlet of the heat exchange jacket and the temperature adjustment flue gas of hot-blast stove
Import is connected, and the outlet of the synthesis gas washing dedusting deacidification system is also connected with the fuel inlet of hot-blast stove.
The 12. moving bed solid waste segmented pyrolysis gasification system as described in claim 10 or 11, it is characterised in that described
Cooling jacket has air intlet and an air outlet slit, and the air intlet is connected with air blower outlet, air outlet slit and hot blast
The air intlet connection of stove.
The 13. moving bed solid waste segmented pyrolysis gasification system as described in claim any one of 9-11, it is characterised in that
The organic matter gasification decomposing system includes that organic matter decomposition gasification device and pyrolysis gas are detained surge tank, the pyrolysis oven epimere
Pyrolysis gas outlet is detained surge tank and is connected with heat recovery system through organic matter decomposition gasification device, pyrolysis gas.
14. moving bed solid waste segmented pyrolysis gasification systems as claimed in claim 13, it is characterised in that described organic
Thing decomposition gasification device is cyclone separator structure, and top is provided with 1-3 burner noz(zle), the middle part of the organic matter decomposition gasification device
Import is connected with pyrolysis oven, and top exit and pyrolysis gas are detained surge tank and are connected, outlet at bottom and the pyrolysis residue cooler
Connection.
15. moving bed solid waste segmented pyrolysis gasification systems as claimed in claim 13, it is characterised in that the pyrolysis
Connecting pipe between stove and organic matter decomposition gasification device has upward inclination angle, and angle is controlled at 30~60 °.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107267176A (en) * | 2017-07-06 | 2017-10-20 | 武汉光谷蓝焰新能源股份有限公司 | A kind of efficient biomass handles tar multi-joint-production pyrolysis oven |
| CN107366914A (en) * | 2017-07-20 | 2017-11-21 | 华中科技大学 | A kind of continous way refuse pyrolysis plant with binder function |
| CN110041949A (en) * | 2019-05-09 | 2019-07-23 | 重庆富燃科技股份有限公司 | A kind of device and method of pair of powdery (or graininess) solid matter recycling treatment |
| CN110898597A (en) * | 2019-12-17 | 2020-03-24 | 山东农洁环保有限公司 | Oxygen-control low-temperature carbonization pyrolysis garbage treatment method |
| CN113883527A (en) * | 2021-10-18 | 2022-01-04 | 西安西热锅炉环保工程有限公司 | Construction waste disposal and resource utilization system and method based on pulverized coal fired boiler |
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2017
- 2017-01-03 CN CN201710000780.3A patent/CN106833690A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107267176A (en) * | 2017-07-06 | 2017-10-20 | 武汉光谷蓝焰新能源股份有限公司 | A kind of efficient biomass handles tar multi-joint-production pyrolysis oven |
| CN107366914A (en) * | 2017-07-20 | 2017-11-21 | 华中科技大学 | A kind of continous way refuse pyrolysis plant with binder function |
| CN107366914B (en) * | 2017-07-20 | 2019-07-05 | 华中科技大学 | A kind of continous way refuse pyrolysis plant with binder function |
| CN110041949A (en) * | 2019-05-09 | 2019-07-23 | 重庆富燃科技股份有限公司 | A kind of device and method of pair of powdery (or graininess) solid matter recycling treatment |
| CN110898597A (en) * | 2019-12-17 | 2020-03-24 | 山东农洁环保有限公司 | Oxygen-control low-temperature carbonization pyrolysis garbage treatment method |
| CN113883527A (en) * | 2021-10-18 | 2022-01-04 | 西安西热锅炉环保工程有限公司 | Construction waste disposal and resource utilization system and method based on pulverized coal fired boiler |
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