CN110437858A - A kind of method and apparatus of the reproducible micro ware auxiliary catalysis fast pyrogenation house refuse of catalyst - Google Patents
A kind of method and apparatus of the reproducible micro ware auxiliary catalysis fast pyrogenation house refuse of catalyst Download PDFInfo
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- CN110437858A CN110437858A CN201910792782.XA CN201910792782A CN110437858A CN 110437858 A CN110437858 A CN 110437858A CN 201910792782 A CN201910792782 A CN 201910792782A CN 110437858 A CN110437858 A CN 110437858A
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- 239000003054 catalyst Substances 0.000 title claims abstract description 111
- 238000006555 catalytic reaction Methods 0.000 title claims abstract description 20
- 238000000034 method Methods 0.000 title claims abstract description 17
- 238000000197 pyrolysis Methods 0.000 claims abstract description 78
- 238000002485 combustion reaction Methods 0.000 claims abstract description 20
- 230000008929 regeneration Effects 0.000 claims abstract description 10
- 238000011069 regeneration method Methods 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims description 40
- 239000000463 material Substances 0.000 claims description 19
- 230000003197 catalytic effect Effects 0.000 claims description 17
- 239000000047 product Substances 0.000 claims description 16
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 14
- 239000003546 flue gas Substances 0.000 claims description 14
- 238000012546 transfer Methods 0.000 claims description 12
- 239000011261 inert gas Substances 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 239000012530 fluid Substances 0.000 claims description 8
- 238000005243 fluidization Methods 0.000 claims description 7
- 239000000446 fuel Substances 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 5
- 238000003860 storage Methods 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 239000006004 Quartz sand Substances 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 3
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical group C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 239000012265 solid product Substances 0.000 claims description 3
- 230000000153 supplemental effect Effects 0.000 claims description 3
- 239000003921 oil Substances 0.000 abstract description 20
- 238000007233 catalytic pyrolysis Methods 0.000 abstract description 4
- 239000012075 bio-oil Substances 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 description 7
- 239000010813 municipal solid waste Substances 0.000 description 5
- 239000002028 Biomass Substances 0.000 description 4
- 238000003763 carbonization Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 230000002779 inactivation Effects 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 238000002161 passivation Methods 0.000 description 3
- 238000010926 purge Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 239000010791 domestic waste Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 206010002660 Anoxia Diseases 0.000 description 1
- 241000976983 Anoxia Species 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 206010021143 Hypoxia Diseases 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000007953 anoxia Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 239000003818 cinder Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000002361 compost Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical class O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000002184 metal Chemical class 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000001698 pyrogenic effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 210000000952 spleen Anatomy 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Classifications
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a kind of method and apparatus of the reproducible micro ware auxiliary catalysis fast pyrogenation house refuse of catalyst, described device includes fluidized bed pyrolysis furnace, microwave generator, the reproducible catalyst bed of catalyst, gs-oil separator, combustion furnace and cyclone separator；Gas access is arranged in fluidized bed pyrolysis furnace bottom, the side wall of fluidized bed pyrolysis furnace and the bottom of catalyst bed or side wall is arranged in microwave generator, the entrance of cyclone separator is connected to the pyrolysis gas outlet of fluidized bed pyrolysis furnace, the gas vent of cyclone separator is connected to catalyst bed, the gas vent of catalyst bed is connected to gs-oil separator, and the outlet of gs-oil separator is connected to the lower part of combustion furnace.The present invention can carry out microwave-assisted fast pyrogenation house refuse and realize catalyst regeneration, the efficiency of catalytic pyrolysis be improved, to improve the yield and quality of bio oil；The energy has been saved while realizing the resource utilization of house refuse, and the service life of device can be effectively improved, it is economic and environment-friendly.
Description
Technical field
The present invention relates to a kind of system of the continuous fast pyrogenation house refuse of producing process more particularly to a kind of catalyst
The method and apparatus of reproducible micro ware auxiliary catalysis fast pyrogenation house refuse.
Background technique
With the quickening of the fast-developing urbanization process of Chinese society economy and the rapid raising of living standards of the people,
City production is also consequently increased rapidly with the junk generated in life process, and house refuse land occupation pollutes environment
Situation and influence to health of people are also all the more obvious.The substantial increase of domestic waste keeps garbage disposal more and more tired
The problems such as difficulty, resultant environmental pollution, gradually has aroused widespread concern in all circles of society.China will realize domestic waste
Industrialization, recycling, minimizing and innoxious, just must be low in face of mixed collection, the content of recyclable materials and calorific value, rubbish
Rubbish moisture content and the high house refuse of biodegradable organic content.For these problems, diversified technology is also applied
And it gives birth to.
The study found that municipal refuse has the characteristics that resource and harmfulness and deposits.For the innoxious place of house refuse
It manages, domestic main mode at present is landfill, burning, compost and pyrolysis.Compared to other processing modes, pyrolysis can make to live
Organic solid waste in rubbish carries out pyrolytic under anaerobic or anoxia condition, and decomposition product is innoxious significant, secondary
It pollutes small, and making full use of for recycling can be carried out, respond the call of energy-saving and emission-reduction, extremely meet nowadays ecological environment guarantor
Protect leading overall situation.
In pyrolytic technique at this stage, microwave-assisted fast pyrogenation is converted as a kind of emerging technology applied to biomass
It is prominent to prepare field of renewable energy advantage, but that there are still calorific values is low, the rate of heat addition is slow, catalyst use efficiency is low etc. is scarce
It falls into, wherein the not high problem of catalyst utilization is especially prominent.During catalytic pyrolysis, if heating rate is lower, reaction temperature
Degree is not high, and the rate of heat addition is slow, biomass material can be made to rest on cold stage, generates a large amount of solid residue；And it is pyrolyzed
Product is easily carbonized, and catalyst bed duct is caused to block, and makes its passivation, inactivation, low so as to cause catalyst use efficiency, makes
The operation and maintenance cost of catalyst bed increases, and economy reduces, and has seriously affected the productivity and yield of product oil.Therefore how
Realize that the optimization and upgrading of catalyst bed becomes urgent problem during catalytic pyrolysis.
Summary of the invention
Low the purpose of the present invention is to solve catalytic efficiency in existing micro ware auxiliary catalysis fast pyrolysis technology
Problem, to provide a kind of method and apparatus of reproducible micro ware auxiliary catalysis fast pyrogenation house refuse of catalyst, energy
It is enough to improve because thermal decomposition product carbonization causes the catalyst of catalyst bed inactivation renewable.
The purpose of the present invention is realized at least through one of following technical scheme.
A kind of device of the reproducible micro ware auxiliary catalysis high temperature pyrolysis house refuse gas of catalyst, including fluid bed heat
Solve furnace, microwave generator, the reproducible catalyst bed of catalyst, gs-oil separator, combustion furnace and cyclone separator；Fluid bed heat
It solves furnace bottom and gas access is set, there is bed material in inside, and the side wall of fluidized bed pyrolysis furnace is arranged in microwave generator and catalyst can
The bottom of regenerated catalyst bed or side wall, the entrance of cyclone separator are connected to the pyrolysis gas outlet of fluidized bed pyrolysis furnace, rotation
The bottom of wind separator is connected to the lower part of fluidized bed pyrolysis furnace, and it is renewable that the gas vent of cyclone separator is connected to catalyst
Catalyst bed, the gas vent of the reproducible catalyst bed of catalyst is connected to gs-oil separator, the outlet of gs-oil separator
It is connected to the lower part of combustion furnace.
Further, the reproducible catalyst bed of the catalyst is divided into catalytic domain and wall type heat transfer zone, and catalyst bed is
Discoid, wall type heat transfer zone is located at the periphery of disk, and catalytic domain is surrounded by wall type heat transfer zone.
Further, wall type heat transfer zone is provided with U-shaped pipe, is easy to implement and is evenly heated, and realizes for heatable catalytic area
Catalyst regeneration and catalysis reaction.
Further, fluidized bed pyrolysis furnace outer wall setting collet is stated, and fills heat exchanging fluid in collet.It is used in the present invention
Flue gas after catalyst bed UTILIZATION OF VESIDUAL HEAT IN is as heat exchanging fluid.
It further, further include the screw feeder and hopper for being convenient for charging, hopper is connected to the charging of screw feeder
Mouthful, the discharge port of screw feeder is connected to fluidized bed pyrolysis furnace, conveys material for fluidized bed pyrolysis furnace.
Further, the exhanst gas outlet of the combustion furnace is connected to the U-shaped pipe of the reproducible catalyst bed of catalyst
Entrance, the outlet of U-shaped pipe are connected to the collet of fluidized bed pyrolysis furnace.
Further, exhanst gas outlet is arranged in the top of fluidized bed pyrolysis furnace, and slag-drip opening is arranged in bottom, and what when pyrolysis generated consolidates
Body residue reaches pyrolysis oven slag-drip opening and is discharged；Supplemental fuel inlet is arranged in the furnace bottom that burns.
The method for carrying out pyrolysis house refuse liquefaction using above-mentioned apparatus, includes the following steps:
(1) house refuse after being dried enters fluidized bed pyrolysis furnace by screw feeder and is pyrolyzed, from bottom
The inert gas and bed material that gas feed is passed through form fluidisation state；For the uniformity for improving heating, the fluidization number of the fluidisation state
It is adjustable, and microwave generator can improve heating rate, quick, the uniform heating in fluidized bed pyrolysis furnace be realized, to ensure to be catalyzed
Bed is in catalytic reaction temperature window；
(2) pyrolysis gas generated after pyrolysis is sent into cyclone separator and carries out separation gas solid separation, and obtained solid product is logical
It crosses returning charge and is transmitted back to fluidized bed pyrolysis furnace, gaseous products enter the reproducible catalyst bed of catalyst and are catalyzed；
(3) the product liquid oil that the gas obtained after being catalyzed is isolated through gs-oil separator is saved with oil storage tank, is not coagulated
Gaseous product is sent into combustion furnace；
(4) flue gas that combustion furnace is drawn provides heat, the reproducible catalyst of catalyst to the reproducible catalyst bed of catalyst
The coke adhered on bed can generate under the high temperature conditions carbon dioxide with oxygen and escape, so as to improve catalyst bed due to carbonization
Caused passivation inactivation, promotes catalyst regeneration；Then it is fluidized bed that the after-heat that flue gas carries, which enters fluidized bed pyrolysis furnace,
Pyrolysis oven heat exchange, reduces the supply of external energy.
Further, it is constantly passed through high temperature inert gas into fluidized bed pyrolysis furnace, pyrolytic reaction is made to be placed in the ring of anaerobic
Border, while inert gas and bed material being made to form stabilization fluid state.
Further, the catalyst after regeneration before the use, is first passed through inert gas and is purged, oxygen is avoided to enter
In catalyst bed.
Further, the bed material is quartz sand, and adds SiC in pyrolysis oven and catalyst bed, is inhaled as microwave
Agent is received, convenient for absorbing microwave, reaches preferably pyrolysis effect.
Further, catalytic temperature is 450-550 DEG C in the reproducible catalyst bed of catalyst.
Further, the flue gas after UTILIZATION OF VESIDUAL HEAT IN leads to flue gas processing device by the fume pipe being connected with pyrolysis oven,
It is outwardly discharged after cleaning.
The present invention has the advantage that compared with prior art
(1) present invention handles house refuse in such a way that one kind is highly efficient, clean, reduces the discharge of pollutant, will live
Garbage as resource utilizes, and can be relieved energy crisis and environmental degradation problem.
(2) microwave-assisted fast warming solution is utilized, microwave-heating technique is strong to the tolerance of water, is not necessarily to predrying, can have
Effect regulation reaction temperature simultaneously causes to be rapidly heated, and convenient for being mentioned by control operating condition such as microwave power, heating temperature etc.
High pyrolysis rate, and then improve the yield of bio oil.Meanwhile the biomass in micro ware auxiliary catalysis pyrolysis house refuse, it can subtract
The carbonisation of few biomass cold stage, catalyst inactivation caused by avoiding material from mixing with catalyst are conducive to improve
The yield and quality of product oil.
(3) catalyst bed is connected to microwave generator, to ensure that catalytic bed in catalytic reaction temperature window, is conducive to improve
Its deactivation prob.
(4) catalyst bed is divided into catalysis, purge zone and wall type heat transfer zone, it can be achieved that one multi-purpose.Pyrolysis gas is by urging
Change region to be catalyzed, and periodically lead to inert gas to the phase and purged, is effectively improved because its hole is blocked in pyrogenic steam carbonization
The problems such as catalyst bed passivation inactivates caused by structure, catalytic efficiency is low is conducive to keep reaction process long-term, steadily high
Effect carries out, and improves the service life of equipment, reduces the operation and maintenance cost of equipment, and economy is high.Meanwhile logical high temperature inert
Gas can promote the regeneration of catalyst, reduces catalyst bed and realizes reproducible cost.In addition, pore structure promotes heating
Uniformity, it is structural good.Catalyst bed bed wall is a U-shaped high-temperature flue gas pipeline of circle, provides heat for catalyst bed, makes it
It is even heated, to promote the renewable of catalyst.
(5) high-temperature flue gas vented one's spleen and generated using the catalytic thermal that combustion furnace burning is collected, to catalyst bed and fluidized bed
Heat required for pyrolysis oven auxiliary provides, reduces the supply of external energy, it can be achieved that resource makes full use of.
In summary, the advantages of the technology of the present invention is simple and easy to do, catalytic pyrolysis is high-efficient, energy conservation and environmental protection, can widely fit
For the processing of house refuse, application prospect is wider.
Detailed description of the invention
Fig. 1 is a kind of process flow signal of reproducible microwave-assisted fast pyrogenation house refuse of catalyst of the present invention
Figure；
Fig. 2 is the detailed construction schematic diagram of catalyst bed；
In figure: 1 screw feeder；2 hoppers；3 microwave generators；4 collets；5 fluidized bed pyrolysis furnaces；6 materials；7 bed materials；8 whirlwind
Separator；9 catalyst beds；10 gs-oil separators；11 oil storage tanks；12 auxiliary fuels；13 combustion furnaces；14 catalysis and catalyst are again
(periodically use inert gas purge) in raw, purge zone；15 high-temperature flue gas pipelines；16 wall-type heat exchange areas.
Specific embodiment
Specific implementation of the invention is described further below in conjunction with specific embodiments and the drawings.
Embodiment
As shown in Figure 1, a kind of device of the reproducible micro ware auxiliary catalysis high temperature pyrolysis gas of catalyst, including fluidized bed
The reproducible catalyst bed 9 of pyrolysis oven 5, microwave generator 3, catalyst, gs-oil separator 10, combustion furnace 13 and cyclone separator
8；Gas access is arranged in 5 bottom of fluidized bed pyrolysis furnace, and there is bed material 7 in inside, and fluidized bed pyrolysis furnace 5 is arranged in microwave generator 3
The bottom or side wall, the entrance of cyclone separator 8 of side wall and the reproducible catalyst bed 9 of catalyst are connected to fluidized bed pyrolysis furnace
5 pyrolysis gas outlet, the bottom of cyclone separator 5 are connected to the lower part of fluidized bed pyrolysis furnace 5, and the gas of cyclone separator 5 goes out
Mouth is connected to the reproducible catalyst bed 9 of catalyst, and the gas vent of the reproducible catalyst bed 9 of catalyst is connected to oil gas point
From device 10, the outlet of gs-oil separator 10 is connected to the lower part of combustion furnace 13.It further include the screw feeder 1 and material convenient for charging
Bucket 2, hopper 2 is connected to the feed inlet of screw feeder 1, and the discharge port of screw feeder 1 is connected to fluidized bed pyrolysis furnace 5, is
Fluidized bed pyrolysis furnace 5 conveys material.
As shown in Fig. 2, the reproducible catalyst bed 9 of catalyst is divided for catalytic domain 14 and wall type heat transfer zone 16, catalysis
Agent bed be it is discoid, wall type heat transfer zone 16 is located at the periphery of disk, and catalytic domain 14 is surrounded by wall type heat transfer zone 16.Wall type heat transfer zone
16 are provided with U-shaped pipe 15, are easy to implement and are evenly heated, and realize catalyst regeneration and catalysis reaction for heatable catalytic area 14.
The exhanst gas outlet of the combustion furnace 13 is connected to the entrance of the U-shaped pipe 15 of the reproducible catalyst bed 9 of catalyst, U-shaped pipe
15 outlet is connected to the collet 4 of fluidized bed pyrolysis furnace 5.Exhanst gas outlet, bottom setting row is arranged in the top of fluidized bed pyrolysis furnace 5
Cinder notch, the solid residue that when pyrolysis generates reach pyrolysis oven slag-drip opening and are discharged；Supplemental fuel inlet is arranged in 13 bottom of combustion furnace
12。
Collet is arranged in 5 outer wall of fluidized bed pyrolysis furnace, and heat exchanging fluid is filled in collet.Using by urging in the present invention
Flue gas after agent bed UTILIZATION OF VESIDUAL HEAT IN is as heat exchanging fluid.
When heat supply is insufficient in pyrolysis oven 5, can be carried out with auxiliary fuel 10 combustion-supporting.
The method for carrying out pyrolysis house refuse gas using above-mentioned apparatus, includes the following steps: as shown in Fig. 1
(1) house refuse after being dried is pyrolyzed by screw feeder 1 into fluidized bed pyrolysis furnace 5, is pyrolyzed
Temperature control have in 500 DEG C, pyrolysis oven 5 bed material 7(include be not limited to catalyst, quartz sand) and microwave absorption it is (suitable
SiC), the inert gas and bed material being passed through from bottom gas inlet form fluidisation state, and the pyrolytic reaction is made to be placed in the item of anaerobic
Under part；
(2) pyrolysis gas generated after pyrolysis is sent into cyclone separator 8 and carries out separation gas solid separation, and obtained solid product is logical
It crosses returning charge and is transmitted back to fluidized bed pyrolysis furnace 5, gaseous products enter the reproducible catalyst bed 9 of catalyst and are catalyzed；
(3) gas obtained after the gas catalysis obtained after being catalyzed enters condenser, that is, is connected with the Oil-gas Separation of condensation working medium
Device 10, condensed product temperatur is lower than the saturation temperature of water at this pressure to prevent in water steam entrained gas.It condenses
To product liquid oil enter in oil storage tank 11 and saved, on-condensible gas product is sent into burner, such as with auxiliary fuel 12
Natural gas burns together；
(4) burning that the liquid product oil in oil storage tank 11 can be used in combustion furnace 13, together with auxiliary fuel 12 such as natural gas
It burns；High-temperature flue gas can be such that the carbon deposit in it aoxidizes under the high temperature conditions by pipeline to catalyst bed 9 simultaneously, promote
Into catalyst regeneration；The gaseous products that cyclone separator is isolated enter catalyst bed and carry out catalytic reforming, catalytic temperature control
At 450-550 DEG C, the microwave generator 3 accessed therewith provides required heat for the auxiliary of catalyst bed 9, to ensure catalytic bed
Layer is in catalytic reaction temperature window；It is transported to fluidized bed pyrolysis furnace 5 again, if the after-heat entrained by it can meet for pyrolysis
The work operation of furnace 5 is supplied, then auxiliary heat supplying again, reduces the supply of external energy.Flue gas after UTILIZATION OF VESIDUAL HEAT IN passes through
The fume pipe being connected with pyrolysis oven leads to flue gas processing device, is outwardly discharged after clean.
Further, the catalyst after regeneration before the use, first leads to inert gas such as nitrogen to catalyst bed 9 and blows
It sweeps, oxygen is avoided to enter in catalyst bed.
Catalyst is attached on the carrier of catalyst bed, and catalyst includes being not limited to: zeolite, metal salt, metal oxide
Or minerals.
Embodiment of the present invention are not limited by the above embodiments, other are any without departing from Spirit Essence of the invention
With changes, modifications, substitutions, combinations, simplifications made under principle, equivalent substitute mode should be, be included in of the invention
Within protection scope.
Claims (10)
1. a kind of device of the reproducible micro ware auxiliary catalysis fast pyrogenation house refuse of catalyst, which is characterized in that including stream
Change bed pyrolysis oven (5), microwave generator (3), the reproducible catalyst bed of catalyst (9), gs-oil separator (10), combustion furnace
(13) and cyclone separator (8)；Gas access is arranged in fluidized bed pyrolysis furnace (5) bottom, and there are bed material (7), microwave generator in inside
(3) setting is in the side wall of fluidized bed pyrolysis furnace (5) and bottom or the side wall of the reproducible catalyst bed of catalyst (9), whirlwind point
Entrance from device (8) is connected to the pyrolysis gas outlet of fluidized bed pyrolysis furnace (5), and the bottom of cyclone separator (5) is connected to fluidisation
The lower part of bed pyrolysis oven (5), the gas vent of cyclone separator (5) are connected to the reproducible catalyst bed of catalyst (9), are catalyzed
The gas vent of the reproducible catalyst bed of agent (9) is connected to gs-oil separator (10), the outlet connection of gs-oil separator (10)
To the lower part of combustion furnace (13).
2. the apparatus according to claim 1, which is characterized in that the reproducible catalyst bed of catalyst (9) is porous
Structure, is divided into catalytic domain (14) and wall type heat transfer zone (16), catalyst bed be it is discoid, wall type heat transfer zone (16) are located at disk
Periphery, catalytic domain (14) are surrounded by wall type heat transfer zone (16).
3. the apparatus of claim 2, which is characterized in that wall-type heat exchange area (16) are provided with U-shaped pipe (15), are used
Catalyst regeneration and catalysis reaction are realized in heatable catalytic area (14).
4. device according to claim 3, which is characterized in that collet is arranged in fluidized bed pyrolysis furnace (5) outer wall, and presss from both sides
Heat exchanging fluid is filled in set.
5. the apparatus according to claim 1, which is characterized in that further include screw feeder (1) and hopper (2), hopper (2)
It is connected to the feed inlet of screw feeder (1), the discharge port of screw feeder (1) is connected to fluidized bed pyrolysis furnace (5), for fluidisation
Bed pyrolysis oven (5) conveys material.
6. device according to claim 4, which is characterized in that the exhanst gas outlet of the combustion furnace (13) is connected to catalyst
The entrance of the U-shaped pipe (15) of reproducible catalyst bed (9), the outlet of U-shaped pipe (15) are connected to fluidized bed pyrolysis furnace (5)
Collet (4).
7. the apparatus according to claim 1, which is characterized in that exhanst gas outlet, bottom is arranged in the top of fluidized bed pyrolysis furnace (5)
Slag-drip opening is arranged in portion；Supplemental fuel inlet (12) are arranged in combustion furnace (13) bottom.
8. a kind of method that the described in any item devices of claim 1-7 carry out fast pyrogenation house refuse, which is characterized in that packet
Include following steps:
(1) house refuse after being dried is pyrolyzed by screw feeder (1) into fluidized bed pyrolysis furnace (5), the bottom of from
The inert gas and bed material that portion's gas feed is passed through form fluidisation state；
(2) pyrolysis gas generated after pyrolysis is sent into cyclone separator (8) and carries out separation gas solid separation, obtained solid product
It is sent back to fluidized bed pyrolysis furnace (5) by returning charge, gaseous products enter the reproducible catalyst bed of catalyst (9) and urged
Change；
(3) the product liquid oil that the gas obtained after being catalyzed obtains after gs-oil separator (10) is protected with oil storage tank (11)
It deposits, on-condensible gas product is sent into combustion furnace (13)；
(4) flue gas that combustion furnace (13) is drawn promotes catalyst regeneration to the reproducible catalyst bed of catalyst (9)；Then flue gas
It is the heat exchange of fluidized bed pyrolysis furnace into fluidized bed pyrolysis furnace (5) collet (4).
9. according to the method described in claim 8, it is characterized in that, the bed material is quartz sand.
10. according to the method described in claim 8, it is characterized in that, catalytic temperature in the reproducible catalyst bed of catalyst (9)
It is 450-550 DEG C.
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