CN206970545U - A kind of system of fluid bed refuse pyrolysis - Google Patents
A kind of system of fluid bed refuse pyrolysis Download PDFInfo
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- CN206970545U CN206970545U CN201720434764.0U CN201720434764U CN206970545U CN 206970545 U CN206970545 U CN 206970545U CN 201720434764 U CN201720434764 U CN 201720434764U CN 206970545 U CN206970545 U CN 206970545U
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 115
- 239000012530 fluid Substances 0.000 title claims abstract description 48
- 239000010813 municipal solid waste Substances 0.000 claims abstract description 152
- 239000002245 particle Substances 0.000 claims abstract description 48
- 230000008018 melting Effects 0.000 claims abstract description 41
- 238000002844 melting Methods 0.000 claims abstract description 41
- 238000001035 drying Methods 0.000 claims description 65
- 239000006200 vaporizer Substances 0.000 claims description 28
- 150000001875 compounds Chemical class 0.000 claims description 18
- 238000009825 accumulation Methods 0.000 claims description 7
- 239000011521 glass Substances 0.000 claims description 2
- 238000000746 purification Methods 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 238000004939 coking Methods 0.000 abstract description 4
- 239000007787 solid Substances 0.000 abstract description 3
- 239000000969 carrier Substances 0.000 abstract description 2
- 239000002994 raw material Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 56
- 239000003921 oil Substances 0.000 description 27
- 238000002309 gasification Methods 0.000 description 16
- 239000000654 additive Substances 0.000 description 7
- 230000000996 additive effect Effects 0.000 description 7
- 239000003054 catalyst Substances 0.000 description 7
- 238000000034 method Methods 0.000 description 7
- 239000000446 fuel Substances 0.000 description 6
- 238000007711 solidification Methods 0.000 description 6
- 230000008023 solidification Effects 0.000 description 6
- 238000006555 catalytic reaction Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 239000000428 dust Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- 229910052782 aluminium Inorganic materials 0.000 description 2
- 239000004411 aluminium Substances 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 210000000952 spleen Anatomy 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 238000011105 stabilization Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- JAQXDZTWVWLKGC-UHFFFAOYSA-N [O-2].[Al+3].[Fe+2] Chemical compound [O-2].[Al+3].[Fe+2] JAQXDZTWVWLKGC-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 229910052906 cristobalite Inorganic materials 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
- 238000009826 distribution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Abstract
The utility model discloses a kind of system of fluid bed refuse pyrolysis, and the system includes rubbish pretreatment unit, fluid bed, red mud pretreatment unit and ash melting stove；Red mud pretreatment unit includes red mud dryer and red mud disintegrating machine；The granulated garbage entrance of the granulated garbage outlet connection fluid bed of rubbish pretreatment unit, the red mud particle entrance of the red mud particle outlet connection fluid bed of red mud disintegrating machine, the lime-ash entrance of the lime-ash outlet connection ash melting stove of fluid bed.The utility model uses solid thermal carriers of the red mud as fluid bed, carries out pyrolysis rubbish, effectively avoids fluidizing the problems such as bad, coking；Caused pyrolysis gas is used as raw material after processing, is ash melting stove heat supply, reduces system energy consumption.
Description
Technical field
The utility model belongs to fixed-end forces technical field, more particularly to a kind of is using what fluid bed carried out refuse pyrolysis
System.
Background technology
In recent years, the trash processing way of more prevalence is rubbish fluidized bed gasification in the world.Fluidized gasification is to lack
The decomposition reaction carried out under the reducing atmosphere of oxygen or anaerobic, it is innoxious thorough, it is unfavorable for generating bioxin.Producing simultaneously has
Artificial combustion gas, fuel oil and the solid carbon of certain calorific value.So refuse pyrolysis has huge potential advantages.But pass through merely
Pyrolysis processing house refuse, higher temperature, high energy consumption are not only needed, and tar caused by pyrolysis can reduce factor of created gase and heat
Efficiency, liquid can be also condensed into low temperature, a series of problems, such as causing air delivering pipeline to block, corrode is combined with water and dust.
Therefore, it is necessary to add catalyst degradation pyrolysis temperature in pyrolytic process, and generator yield is improved.But traditional catalyst such as calcium
Base catalyst, nickel-base catalyst etc. are expensive, and application cost is higher, and deactivation prob be present, so more difficult trying on a large scale
Test and be applied in producing.It is a current problem for being badly in need of solving to seek cheap catalyst.
The contaminative waste residue that red mud is discharged when being aluminium industry extraction aluminum oxide, average often produces 1t aluminum oxide, attached
Band produces 1.0~2.0t red muds.Along with the production of aluminium, substantial amounts of red mud cannot get sufficiently effective utilization, can only rely on big
The stockyard of area is stacked, and occupies a large amount of soils, serious pollution is also caused to environment.
Utility model content
In order to solve the above problems, the utility model proposes a kind of system using fluidized bed pyrolysis gasification process rubbish,
Using red mud catalysis refuse pyrolysis gasification, refuse pyrolysis gasification energy consumption, tar yield pole in refuse pyrolysis gasification are reduced
It is low, the problems such as avoiding tar coking, blocking pipeline.
The utility model provides a kind of system of fluid bed refuse pyrolysis, including rubbish pretreatment unit, fluid bed, red mud
Pretreatment unit and ash melting stove；
The rubbish pretreatment unit includes garbage inlet and granulated garbage exports；
The fluid bed includes pyrolysis vaporizer, the pyrolysis vaporizer be provided with granulated garbage entrance, red mud particle entrance,
Pyrolysis gas outlet and lime-ash outlet；
The red mud pretreatment unit includes red mud dryer and red mud disintegrating machine；
The red mud dryer includes red mud entrance and dry red mud exports；
The red mud disintegrating machine includes dry red mud entrance and red mud particle outlet, the dry red mud outlet of the red mud dryer
Connect the dry red mud entrance of the red mud disintegrating machine；
The ash melting stove includes lime-ash entrance and vitreum exports；
The granulated garbage outlet of the rubbish pretreatment unit connects the granulated garbage entrance of the fluid bed, the red mud
The red mud particle outlet of disintegrating machine connects the red mud particle entrance of the fluid bed, and the lime-ash of the fluid bed is exported described in connection
The lime-ash entrance of ash melting stove.
As the preferable scheme of the utility model, the rubbish pretreatment unit include rubbish drying machine, refuse grinder,
Kneader and comminutor,
The rubbish drying machine includes garbage inlet and garbage drying exports；
The refuse grinder includes garbage drying entrance and shredding refuse exports；
The kneader includes shredding refuse entrance and compound exports；
The comminutor includes compound entrance and granulated garbage exports；
The garbage drying outlet of the rubbish drying machine connects the garbage drying entrance of the refuse grinder, the rubbish
The shredding refuse outlet of disintegrating machine connects the shredding refuse entrance of the kneader, the compound outlet connection institute of the kneader
The compound entrance of comminutor is stated, the granulated garbage outlet of the comminutor connects the granulated garbage entrance of the fluid bed.
System of the present utility model further comprises First Heat Exchanger, and the First Heat Exchanger includes vitreum entrance and changed
Hot oil outlet, the rubbish drying machine are provided with heat exchange oil-in, the vitreum outlet connection described first of the ash melting stove
The vitreum entrance of heat exchanger, the heat exchange oil export of the First Heat Exchanger connect the heat exchange oil-in of the rubbish drying machine.
As preferable scheme, system of the present utility model also includes pyrolysis gas clean unit, and the pyrolysis gas purification is single
Member includes purifier, and the purifier includes pyrolysis gas entrance and combustible gas exports；The ash melting stove is provided with accumulation of heat
Formula radiant tube；The pyrolysis gas outlet of the fluid bed connects the pyrolysis gas entrance of the purifier, the purifier can
Gas outlet connects the heat accumulation type radiant tube of the ash melting stove.
Further, the pyrolysis gas clean unit also includes the second heat exchanger, and second heat exchanger includes high temperature
Pyrolysis gas entrance, Low Temperature Thermal outlet and heat exchange oil export, the red mud dryer are provided with heat exchange oil-in, the fluid bed
Pyrolysis gas outlet connect the high temperature pyrolysis gas entrance of second heat exchanger, the Low Temperature Thermal outlet of second heat exchanger
The pyrolysis gas entrance of the purifier is connected, the heat exchange oil export of second heat exchanger connects changing for the red mud dryer
Deep fat entrance.
System provided by the utility model using fluidized bed pyrolysis rubbish, using red mud catalysis refuse pyrolysis gasification, drop
Low refuse pyrolysis gasification energy consumption, saves process costs, improves gasification gas yield and quality；In refuse pyrolysis gasification
Tar yield is extremely low, the problems such as avoiding tar coking, blocking pipeline；Utilize internal system residual heat drying red mud and rubbish, drop
The low energy consumption of whole system；Lime-ash is handled in ash melting stove, realizes the stabilization processes of danger wastes.
Brief description of the drawings
Fig. 1 is the system schematic of the utility model embodiment；
Fig. 2 is the method flow diagram of the pyrolysis rubbish of the utility model embodiment.
In figure：
1- rubbish pretreatment unit, 11- rubbish drying machines, 12- refuse grinders, 13- kneaders, 14- comminutors, 15-
Garbage feeding machine；
2- fluid beds；
3- red muds pretreatment unit, 31- red muds dryer, 32- red mud disintegrating machines；
4- ash melting stoves；
5- First Heat Exchangers；
6- pyrolysis apparatus clean unit, the heat exchangers of 61- second, 62- purifiers.
Embodiment
Below in conjunction with drawings and examples, specific embodiment of the present utility model is described in more details, with
Just the advantages of better understood when scheme and its various aspects of the present utility model.However, specific implementations described below side
Formula and embodiment are for illustrative purposes only, rather than to limitation of the present utility model.
As shown in figure 1, the utility model embodiment provides a kind of system of fluid bed refuse pyrolysis, including rubbish pretreatment
Unit 1, fluid bed 2, red mud pretreatment unit 3, ash melting stove 4, First Heat Exchanger 5 and pyrolysis apparatus clean unit 6.This practicality
New embodiment provides a kind of new way using Industrial Solid Waste red mud catalysis pyrolysis house refuse for urban garbage disposal
Footpath.
Rubbish can be processed into the granulated garbage available for pyrolysis by rubbish pretreatment unit 1.Rubbish pretreatment unit 1 includes
Rubbish drying machine 11, refuse grinder 12, kneader 13, comminutor 14 and garbage feeding machine 15.
Rubbish drying machine 11 is used for the drying of rubbish, and rubbish can be dried to moisture content below 10%.Rubbish drying machine
11 include garbage inlet and garbage drying outlet.
Refuse grinder 12 includes garbage drying entrance and shredding refuse exports, the garbage drying outlet of rubbish drying machine 11
Connect the garbage drying entrance of refuse grinder 12.The garbage drying of rubbish drying machine 11 delivers to refuse grinder by conveyer belt
12, garbage drying is crushed to 10~20mm by refuse grinder 12.
Kneader 13 includes shredding refuse entrance and compound exports, and the shredding refuse outlet connection of refuse grinder 12 is pinched
The shredding refuse entrance of conjunction machine 13.Additive entrance is additionally provided with kneader 13, the function of additive is rubbish is possessed necessarily
Caking property, additive fully mixed with rubbish by kneader 13, obtains compound.
Comminutor 14 includes compound entrance and granulated garbage exports, the compound outlet connection comminutor 14 of kneader 13
Compound entrance.The compound that kneader 13 manufactures is delivered in comminutor 14, makes growth 30mm, diameter 10mm's is bar-shaped
Granulated garbage.
Garbage feeding machine 15 is located at the lower section of comminutor 14, and the granulated garbage that comminutor 14 is discharged is delivered into fluid bed 2.
Fluid bed 2 includes pyrolysis vaporizer, and non-closed annular heat accumulating type is longitudinally provided with the inside of the furnace wall of pyrolysis vaporizer
Radiant tube, heat energy needed for pyrolytic gasification is provided for pyrolysis vaporizer.The middle part of pyrolysis vaporizer is provided with granulated garbage entrance, rubbish
The granulated garbage that charger 15 conveys enters pyrolysis vaporizer by granulated garbage entrance.Red mud particle entrance is located at granulated garbage
The lower section of entrance, the charging for red mud particle.The bottom of fluid bed 2 is air compartment and air distribution plate, and wind-force medium is nitrogen.Fluidisation
Granulated garbage in bed 2, under the catalytic action of red mud particle, generate pyrolysis gas and lime-ash.Pyrolysis gas and lime-ash pass through respectively
Pyrolysis gas outlet and lime-ash outlet discharge pyrolysis vaporizer.
Red mud pretreatment unit 3 is used for the red mud that will industrially discharge, and is processed into the red mud particle available for fluid bed.It is red
Mud both as the solid thermal carriers for being pyrolyzed rubbish, can be catalyzed refuse pyrolysis again.Red mud pretreatment unit 3 includes red mud dryer
31 and red mud disintegrating machine 32.
The moisture content of red mud can be down to less than 30% by red mud dryer 31, and it includes red mud entrance and the outlet of dry red mud.
Red mud disintegrating machine 32 includes dry red mud entrance and red mud particle outlet, the dry red mud outlet connection of red mud dryer 31
The dry red mud entrance of red mud disintegrating machine 32.After dry red mud enters red mud disintegrating machine 32 by red mud dryer 31, particle diameter is crushed to
For 10~15mm.Red mud particle after broken is by the red mud particle entrance of fluid bed 2, into pyrolysis vaporizer.
Ash melting stove 4 includes lime-ash entrance and vitreum exports, the lime-ash outlet connection ash melting stove 4 of fluid bed 2
Lime-ash entrance.Ash melting stove 4 is heated using heat accumulation type radiant tube, after hot lime-ash enters ash melting stove, 1400~
Melting and solidification under 1900 DEG C of hot conditions, ultimately becomes vitreum, realizes to harmful heavy metal stabilization treatment in lime-ash.
First Heat Exchanger 5 includes vitreum entrance and heat exchange oil export, the vitreum outlet connection first of ash melting stove 2
The vitreum entrance of heat exchanger 5.The high temp glass body that ash melting stove 2 is discharged enters First Heat Exchanger 5, enters in the ranks with heat exchange oil
Connect heat exchange.Rubbish drying machine 11 is provided with heat exchange oil-in, and the heat exchange oil export connection rubbish drying machine 11 of First Heat Exchanger 5 changes
Deep fat entrance.The high temperature heat exchange oil of First Heat Exchanger 5, into rubbish drying machine 11, the thermal source as drying garbage.
Pyrolysis gas clean unit 6 includes the second heat exchanger 61 and purifier 62, for the waste heat recovery of pyrolysis gas and net
Change.
Second heat exchanger 61 includes high temperature pyrolysis gas entrance, Low Temperature Thermal outlet and heat exchange oil export, the heat of fluid bed 2
Vent one's spleen and export the high temperature pyrolysis gas entrance of the second heat exchanger 61 of connection.Pyrolysis gas temperature is very high caused by fluid bed 2, and pyrolysis gas enters
Enter the second heat exchanger 61 with and deep fat exchanged heat, pyrolysis gas temperature is down to 150 DEG C, realizes waste heat recovery.Red mud dryer
31 are provided with heat exchange oil-in, the heat exchange oil-in of the heat exchange oil export connection red mud dryer 31 of the second heat exchanger 61.Second changes
The high temperature heat exchange oil of hot device 61 enters red mud dryer 31, the thermal source as red mud drying.
Purifier 62 includes pyrolysis gas entrance and combustible gas exports, the Low Temperature Thermal outlet connection of the second heat exchanger 61
The pyrolysis gas entrance of purifier 62.In the utility model embodiment, purifier 62 is cyclone dust collectors, can remove pyrolysis gas
In flying dust, obtain combustible gas.Combustible gas is respectively fed to the heat accumulation type radiant tube of fluid bed 2 and the heat accumulating type of ash melting stove 4
Radiant tube, as fuel, energy is provided for whole system.Flying dust is admitted to ash melting stove 4, the melting and solidification together with lime-ash,
Generate vitreum.
In the utility model embodiment, red mud is catalyzed rubbish, the wherein primary chemical of red mud forms as catalyst
For：CaO accounts for total amount 30%~40%, SiO215%~20% is accounted for, iron-aluminium oxide respectively accounts for 10% or so, and also NiO etc. is a small amount of
Other metal oxides；CaO, Fe in red mud2O3, NiO can be with decomposing organic matter and pyrolysis fuel oil, mainly due to alkaline gold
Belong to the pi-electron cloud stability in oxide influence organic matter volatile matter and tar component, so as to reduce the work of its cracking reaction
Changing can so that tar is further cracked into micro-molecular gas.SiO present in red mud simultaneously2、Fe2O3It is also good Deng material
Carrier, the alkaline metal oxide that effectively can be fixed in red mud, prevent from damaging with the dissipation of pyrolysis gas during pyrolytic gasification
Lose.In addition, red mud can after heat treatment form loose structure, so as to increase the specific surface area of red mud, further increase red
The effect of mud catalysis.In order to reduce the content of tar in refuse pyrolysis product, conventional refuse pyrolysis gasification temperature is at 1000 DEG C
More than, by the use of red mud as the catalyst of refuse pyrolysis, the temperature needed for refuse pyrolysis can be effectively reduced, reduces system energy consumption.
As shown in Fig. 2 on the other hand, the utility model embodiment offer is a kind of to carry out refuse pyrolysis using said system
Method, comprise the following steps：
1st, rubbish is sent into rubbish drying machine, rubbish is dried, obtain garbage drying, the moisture content of garbage drying≤
10%.
2nd, garbage drying is sent into refuse grinder, obtains shredding refuse after broken, the particle diameter of shredding refuse for 10~
20mm。
3rd, shredding refuse is mixed in kneader with additive, obtains compound.
4th, comminutor is fed the mixture into, obtains granulated garbage.
5th, crushed after red mud is dried, obtain red mud particle, the particle diameter of red mud particle is 10~15mm.
The 6th, red mud particle is sent into the pyrolysis vaporizer of fluid bed, red mud particle is into fluidised form under wind-force effect.
7th, granulated garbage is sent into pyrolysis vaporizer, pyrolysis vaporizer by the temperature of pyrolysis vaporizer at 800~1000 DEG C
The mass ratio of interior granulated garbage and red mud particle is 1:4~1:10, granulated garbage is pyrolyzed in pyrolysis vaporizer, produces heat
Vent one's spleen and lime-ash.
8th, lime-ash is sent into ash melting stove, the melting and solidification under conditions of 1400~1900 DEG C, obtains vitreum.
9th, vitreum is sent into First Heat Exchanger, exchanged heat with heat exchange oil, the heat exchange oil after First Heat Exchanger is heated up
Rubbish drying machine is delivered to, the thermal source as garbage drying.
10th, pyrolysis gas is sent into the second heat exchanger, is exchanged heat with heat exchange oil, obtain Low Temperature Thermal；By the second heat exchange
Heat exchange oil after device heating is delivered to red mud dryer, as the thermal source for drying red mud.
11st, Low Temperature Thermal feeding purifier is purified, obtains combustible gas；By combustible gas be delivered to fluid bed and
Ash melting stove, as fuel.
The system and method for the refuse pyrolysis of the utility model embodiment, the catalysis of refuse pyrolysis is used as by the use of solid waste red mud
Agent, reduce the cost of processing rubbish；Red mud can improve the quality of pyrolysis gas, reduce tar yield, avoid tar coking, block up
Fill in pipeline；The waste heat of vitreum and pyrolysis gas, garbage drying and red mud are reclaimed, reduces the energy consumption of whole system；Fluid bed and
Ash melting stove is heated using heat accumulation type radiant tube, by the use of refuse pyrolysis gasify caused by low heat value combustible gas as fuel,
Reduce system operation cost.
Embodiment 1
1st, rubbish is sent into rubbish drying machine, rubbish is dried, obtain garbage drying, the moisture content of garbage drying
10%.
2nd, garbage drying is sent into refuse grinder, obtains shredding refuse after broken, the particle diameter of shredding refuse is 15mm.
3rd, shredding refuse is mixed in kneader with additive, obtains compound.
4th, comminutor is fed the mixture into, obtains granulated garbage.
5th, crushed after red mud is dried, obtain red mud particle, the particle diameter of red mud particle is 10mm.
The 6th, red mud particle is sent into the pyrolysis vaporizer of fluid bed, red mud particle is into fluidised form under wind-force effect.
7th, the temperature of pyrolysis vaporizer is at 800 DEG C, granulated garbage is sent into pyrolysis vaporizer, the rubbish in pyrolytic gasification room
The mass ratio of rubbish particle and red mud particle is 1:4, granulated garbage is pyrolyzed in pyrolysis vaporizer, produces pyrolysis gas and lime-ash.
8th, lime-ash is sent into ash melting stove, the melting and solidification under conditions of 1500 DEG C, obtains vitreum.
9th, vitreum is sent into First Heat Exchanger, exchanged heat with heat exchange oil, the heat exchange oil after First Heat Exchanger is heated up
Rubbish drying machine is delivered to, the thermal source as garbage drying.
10th, pyrolysis gas is sent into the second heat exchanger, is exchanged heat with heat exchange oil, obtain Low Temperature Thermal；By the second heat exchange
Heat exchange oil after device heating is delivered to red mud dryer, as the thermal source for drying red mud.
11st, Low Temperature Thermal feeding purifier is purified, obtains combustible gas；By combustible gas be delivered to fluid bed and
Ash melting stove, as fuel.
In the utility model embodiment, pyrolysis gas each component volume fraction caused by pyrolysis oven is H2:35%, CH4:17%,
CO:20%, gas gross calorific value is 4700kcal/m3。
Embodiment 2
1st, rubbish is sent into rubbish drying machine, rubbish is dried, obtain garbage drying, the moisture content of garbage drying
9%.
2nd, garbage drying is sent into refuse grinder, obtains shredding refuse after broken, the particle diameter of shredding refuse is 10mm.
3rd, shredding refuse is mixed in kneader with additive, obtains compound.
4th, comminutor is fed the mixture into, obtains granulated garbage.
5th, crushed after red mud is dried, obtain red mud particle, the particle diameter of red mud particle is 15mm.
The 6th, red mud particle is sent into the pyrolysis vaporizer of fluid bed, red mud particle is into fluidised form under wind-force effect.
7th, the temperature of pyrolysis vaporizer is at 900 DEG C, granulated garbage is sent into pyrolysis vaporizer, the rubbish in pyrolytic gasification room
The mass ratio of rubbish particle and red mud particle is 1:6, granulated garbage is pyrolyzed in pyrolysis vaporizer, produces pyrolysis gas and lime-ash.
8th, lime-ash is sent into ash melting stove, the melting and solidification under conditions of 1400 DEG C, obtains vitreum.
9th, vitreum is sent into First Heat Exchanger, exchanged heat with heat exchange oil, the heat exchange oil after First Heat Exchanger is heated up
Rubbish drying machine is delivered to, the thermal source as garbage drying.
10th, pyrolysis gas is sent into the second heat exchanger, is exchanged heat with heat exchange oil, obtain Low Temperature Thermal；By the second heat exchange
Heat exchange oil after device heating is delivered to red mud dryer, as the thermal source for drying red mud.
11st, Low Temperature Thermal feeding purifier is purified, obtains combustible gas；By combustible gas be delivered to fluid bed and
Ash melting stove, as fuel.
In the utility model embodiment, pyrolysis gas each component volume fraction caused by pyrolysis oven is H2:37%, CH4:22%,
CO:15%, gas gross calorific value is 4460kcal/m3。
Embodiment 3
1st, rubbish is sent into rubbish drying machine, rubbish is dried, obtain garbage drying, the moisture content of garbage drying
8%.
2nd, garbage drying is sent into refuse grinder, obtains shredding refuse after broken, the particle diameter of shredding refuse is 20mm.
3rd, shredding refuse is mixed in kneader with additive, obtains compound.
4th, comminutor is fed the mixture into, obtains granulated garbage.
5th, crushed after red mud is dried, obtain red mud particle, the particle diameter of red mud particle is 12mm.
The 6th, red mud particle is sent into the pyrolysis vaporizer of fluid bed, red mud particle is into fluidised form under wind-force effect.
7th, the temperature of pyrolysis vaporizer is at 1000 DEG C, granulated garbage is sent into pyrolysis vaporizer, in pyrolytic gasification room
The mass ratio of granulated garbage and red mud particle is 1:10, granulated garbage is pyrolyzed in pyrolysis vaporizer, produces pyrolysis gas and ash
Slag.
8th, lime-ash is sent into ash melting stove, the melting and solidification under conditions of 1900 DEG C, obtains vitreum.
9th, vitreum is sent into First Heat Exchanger, exchanged heat with heat exchange oil, the heat exchange oil after First Heat Exchanger is heated up
Rubbish drying machine is delivered to, the thermal source as garbage drying.
10th, pyrolysis gas is sent into the second heat exchanger, is exchanged heat with heat exchange oil, obtain Low Temperature Thermal；By the second heat exchange
Heat exchange oil after device heating is delivered to red mud dryer, as the thermal source for drying red mud.
11st, Low Temperature Thermal feeding purifier is purified, obtains combustible gas；By combustible gas be delivered to fluid bed and
Ash melting stove, as fuel.
In the utility model embodiment, pyrolysis gas each component volume fraction caused by pyrolysis oven is H2:39%, CH4:19%,
CO:8%, gas gross calorific value is 4380kcal/m3。
It should be noted that each embodiment above by reference to described by accompanying drawing is only illustrating the utility model rather than limit
The scope of the utility model processed, it will be understood by those within the art that, do not departing from spirit of the present utility model and model
The modification carried out on the premise of enclosing to the utility model or equivalent substitution, all should cover within the scope of the utility model.
In addition, signified outer unless the context, the word occurred in the singular includes plural form, and vice versa.In addition, except non-specifically
Explanation, then all or part of of any embodiment can combine all or part of of any other embodiment and use.
Claims (5)
1. a kind of system of fluid bed refuse pyrolysis, it is characterised in that locate in advance including rubbish pretreatment unit, fluid bed, red mud
Manage unit and ash melting stove；
The rubbish pretreatment unit includes garbage inlet and granulated garbage exports；
The fluid bed includes pyrolysis vaporizer, and the pyrolysis vaporizer is provided with granulated garbage entrance, red mud particle entrance, pyrolysis
Gas exports and lime-ash outlet；
The red mud pretreatment unit includes red mud dryer and red mud disintegrating machine；
The red mud dryer includes red mud entrance and dry red mud exports；
The red mud disintegrating machine includes dry red mud entrance and red mud particle outlet, the dry red mud outlet connection of the red mud dryer
The dry red mud entrance of the red mud disintegrating machine；
The ash melting stove includes lime-ash entrance and vitreum exports；
The granulated garbage outlet of the rubbish pretreatment unit connects the granulated garbage entrance of the fluid bed, and the red mud crushes
The red mud particle outlet of machine connects the red mud particle entrance of the fluid bed, and the lime-ash outlet of the fluid bed connects the lime-ash
The lime-ash entrance of melting furnace.
2. system according to claim 1, it is characterised in that the rubbish pretreatment unit includes rubbish drying machine, rubbish
Rubbish disintegrating machine, kneader and comminutor,
The rubbish drying machine includes garbage inlet and garbage drying exports；
The refuse grinder includes garbage drying entrance and shredding refuse exports；
The kneader includes shredding refuse entrance and compound exports；
The comminutor includes compound entrance and granulated garbage exports；
The garbage drying outlet of the rubbish drying machine connects the garbage drying entrance of the refuse grinder, the refuse breaking
The shredding refuse outlet of machine connects the shredding refuse entrance of the kneader, is made described in the compound outlet connection of the kneader
The compound entrance of grain machine, the granulated garbage outlet of the comminutor connect the granulated garbage entrance of the fluid bed.
3. system according to claim 2, it is characterised in that further comprise First Heat Exchanger, the First Heat Exchanger
Including vitreum entrance and heat exchange oil export, the rubbish drying machine is provided with heat exchange oil-in, the glass of the ash melting stove
Body outlet connects the vitreum entrance of the First Heat Exchanger, and the heat exchange oil export of the First Heat Exchanger connects the rubbish and done
The heat exchange oil-in of dry machine.
4. system according to claim 1, it is characterised in that further comprise pyrolysis gas clean unit, the pyrolysis gas
Clean unit includes purifier, and the purifier includes pyrolysis gas entrance and combustible gas exports；The ash melting stove is set
There is heat accumulation type radiant tube；The pyrolysis gas outlet of the fluid bed connects the pyrolysis gas entrance of the purifier, the purification dress
The combustible gas outlet put connects the heat accumulation type radiant tube of the ash melting stove.
5. system according to claim 4, it is characterised in that the pyrolysis gas clean unit also includes the second heat exchanger,
Second heat exchanger includes high temperature pyrolysis gas entrance, Low Temperature Thermal outlet and heat exchange oil export, the red mud dryer and set
There is a heat exchange oil-in, the pyrolysis gas outlet of the fluid bed connects the high temperature pyrolysis gas entrance of second heat exchanger, and described the
The Low Temperature Thermal outlet of two heat exchangers connects the pyrolysis gas entrance of the purifier, and the heat exchange oil of second heat exchanger goes out
Mouth connects the heat exchange oil-in of the red mud dryer.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720434764.0U CN206970545U (en) | 2017-04-24 | 2017-04-24 | A kind of system of fluid bed refuse pyrolysis |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720434764.0U CN206970545U (en) | 2017-04-24 | 2017-04-24 | A kind of system of fluid bed refuse pyrolysis |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106987280A (en) * | 2017-04-24 | 2017-07-28 | 北京神源环保有限公司 | A kind of system and method for fluid bed refuse pyrolysis |
| CN113201358A (en) * | 2021-06-09 | 2021-08-03 | 浙江大学 | Method for producing combustible gas by reducing red mud by using organic solid waste pyrolysis gas |
-
2017
- 2017-04-24 CN CN201720434764.0U patent/CN206970545U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106987280A (en) * | 2017-04-24 | 2017-07-28 | 北京神源环保有限公司 | A kind of system and method for fluid bed refuse pyrolysis |
| CN113201358A (en) * | 2021-06-09 | 2021-08-03 | 浙江大学 | Method for producing combustible gas by reducing red mud by using organic solid waste pyrolysis gas |
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