CN109722311A - A kind of device and method cracking the combustion gas of flammable solid waste with fluid bed heat - Google Patents
A kind of device and method cracking the combustion gas of flammable solid waste with fluid bed heat Download PDFInfo
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- CN109722311A CN109722311A CN201910124961.6A CN201910124961A CN109722311A CN 109722311 A CN109722311 A CN 109722311A CN 201910124961 A CN201910124961 A CN 201910124961A CN 109722311 A CN109722311 A CN 109722311A
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- 238000005336 cracking Methods 0.000 title claims abstract description 82
- 239000000567 combustion gas Substances 0.000 title claims abstract description 62
- 238000000034 method Methods 0.000 title claims abstract description 25
- 239000002910 solid waste Substances 0.000 title claims abstract description 21
- 239000012530 fluid Substances 0.000 title claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 145
- 239000007789 gas Substances 0.000 claims abstract description 108
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 69
- 239000000463 material Substances 0.000 claims abstract description 63
- 238000005243 fluidization Methods 0.000 claims abstract description 54
- 230000035939 shock Effects 0.000 claims abstract description 25
- 239000000203 mixture Substances 0.000 claims abstract description 24
- 239000000428 dust Substances 0.000 claims abstract description 22
- 238000010504 bond cleavage reaction Methods 0.000 claims abstract description 20
- 230000007017 scission Effects 0.000 claims abstract description 20
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims abstract description 16
- 229910052700 potassium Inorganic materials 0.000 claims abstract description 16
- 239000011591 potassium Substances 0.000 claims abstract description 16
- 230000009471 action Effects 0.000 claims abstract description 10
- 238000004227 thermal cracking Methods 0.000 claims abstract 2
- 238000009835 boiling Methods 0.000 claims description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 26
- 230000008569 process Effects 0.000 claims description 15
- 230000000694 effects Effects 0.000 claims description 14
- 239000002028 Biomass Substances 0.000 claims description 13
- 239000008246 gaseous mixture Substances 0.000 claims description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 12
- 238000009833 condensation Methods 0.000 claims description 11
- 230000005494 condensation Effects 0.000 claims description 11
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 10
- 229910052751 metal Inorganic materials 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 9
- 230000011218 segmentation Effects 0.000 claims description 7
- 239000002893 slag Substances 0.000 claims description 7
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- 238000009826 distribution Methods 0.000 claims description 4
- 230000005484 gravity Effects 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 4
- 229920000642 polymer Polymers 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 4
- 238000010079 rubber tapping Methods 0.000 claims description 3
- 239000013049 sediment Substances 0.000 claims description 3
- 239000003034 coal gas Substances 0.000 claims description 2
- 238000000197 pyrolysis Methods 0.000 claims description 2
- 230000035484 reaction time Effects 0.000 claims description 2
- 230000000630 rising effect Effects 0.000 claims description 2
- 229910052783 alkali metal Inorganic materials 0.000 abstract description 12
- 150000001340 alkali metals Chemical class 0.000 abstract description 12
- 239000002737 fuel gas Substances 0.000 abstract description 11
- BITYAPCSNKJESK-UHFFFAOYSA-N potassiosodium Chemical compound [Na].[K] BITYAPCSNKJESK-UHFFFAOYSA-N 0.000 abstract description 5
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000011734 sodium Substances 0.000 abstract description 4
- 229910052708 sodium Inorganic materials 0.000 abstract description 4
- 238000002309 gasification Methods 0.000 abstract 1
- 238000007711 solidification Methods 0.000 abstract 1
- 230000008023 solidification Effects 0.000 abstract 1
- 238000012545 processing Methods 0.000 description 6
- 239000002994 raw material Substances 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- 238000013459 approach Methods 0.000 description 2
- 238000000889 atomisation Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000010849 combustible waste Substances 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 2
- 239000010931 gold Substances 0.000 description 2
- 229910052737 gold Inorganic materials 0.000 description 2
- 239000010813 municipal solid waste Substances 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
Landscapes
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention discloses a kind of apparatus and method for cracking the combustion gas of flammable solid waste with fluid bed heat, device is made of fluidisation heat scission reaction producer, grey pulp separator, dust sender, alkali metal potassium sodium condenser.Method are as follows: light material and heavier feeds are added mouth in the light material addition mouth and heavier feeds of fluidisation heat scission reaction producer and are separately added into, and make light material and heavier feeds complete thermal cracking gasification reaction in furnace with the high temperature that combustion gas pure oxygen burner high-temp combustion gas and superheated steam pure oxygen mixture gas nozzle generate；High-temperature fuel gas is under the action of cold shock gas in alkali metal potassium sodium coagulator; alkali metal potassium, sodium in high-temperature gas condense and form solid-state together with net dust bonding with not separating in gas phase; be easily isolated, with protect equipment from alkali metal potassium sodium on it bond solidification when caused by damage.Fuel gases calorific value produced by the invention is high, and lime-ash clinker ignition loss is low, without secondary pollution in production process.
Description
Technical field
The present invention relates to a kind of with the device and method of fluid bed heat cracking flammable solid waste combustion gas.
Background technique
Flammable solid waste is varied, has agricultural solid waste and life solid combustible wastes etc., such as agricultural
Flammable solid waste is mostly agricultural-forestry biomass, and life solid combustible wastes are the combustible in house refuse.It is flammable at present
The processing method of solid waste is all to use air as gasifying agent, and boiler for producing goes out steam and generated electricity with steam turbine generator.Life
Rubbish uses this processing method, and there are following problems: the complex process equipment of fume treatment, the thermal efficiency are low；And it is raw
Garbage disposal living brings dioxin and heavy metal dusts secondary pollution；Simultaneously because the alkali metal gas in high-temperature flue gas is in steam
It is solidified on the heat exchange equipments such as boiler, heat exchange efficiency, safety in production and the service life of heat exchanging equipment all have a great impact.
Summary of the invention
The present invention is for disadvantage present in background technique and problem is improved and innovated, and it is an object of the present invention to provide a kind of use
Fluid bed heat cracks the apparatus and method of flammable solid waste combustion gas, produce it is a kind of without containing dioxin, without tar, no
High heating value combustion gas containing dust.The thermal efficiency is high, and without secondary pollution, boiler ash sediment clinker ignition loss is low.And eliminate alkali metal exchange
The heat exchange efficiency of hot equipment, safety in production and service life influence.
The technical solution adopted by the invention is as follows: a kind of with the dress of fluid bed heat cracking flammable solid waste combustion gas
It sets, it is characterised in that: be made of fluidisation heat scission reaction producer, grey pulp separator, dust sender and potassium soda metal condensation device；
The upper outlet pipeline of the fluidisation heat scission reaction furnace is connect with grey pulp separator import；The lime-ash of grey pulp separator exports
Pipe is connected with dust sender, so that dust sender is connected with boiler ash sediment boiling fluidized reaction section with dust sender Ash water pipe；Lime-ash separation
Device gas outlet pipeline is connect with potassium soda metal condensation device import；Potassium soda metal condensation device is additionally provided with cold shock gas inlet pipe
With gas outlet pipe；The fluidisation heat scission reaction producer is segmentation fluidisation heat scission reaction producer or fluid bed heat cracking
React producer；
The segmentation fluidisation heat scission reaction producer that the present invention uses is divided into lime-ash boiling fluidized reaction section, heavy object from bottom to top
Expect cracking reaction section, light material cracking reaction section, is equipped with bellows in the lower part of lime-ash boiling fluidized reaction section, bellows are equipped with pure
The distribution grid of oxygen superheated steam gaseous mixture blast pipe, bellows top is equipped with multiple blast caps, and bottom is to have slag tapping equipment；In weight
Matter material cracking conversion zone middle and lower part is equipped with two layers of combustion gas pure oxygen high temperature burner, and light material cracking reaction pars infrasegmentalis is equipped with heavy
Mouth is added in material, and the lower part that mouth is added in heavier feeds is equipped with superheated steam pure oxygen mixture gas nozzle；The upper of mouth is added in heavier feeds
Portion is equipped with combustion gas pure oxygen high temperature burner, and the top of combustion gas pure oxygen high temperature burner is equipped with light material and mouth is added, splits in light material
The top of solution fluidisation section is equipped with 1-2 layers of superheated steam pure oxygen mixture gas nozzle.
Flammable solid waste is divided into heavier feeds and light material by the processing of the selection by winnowing in Raw material processing stage, and by two
Kind material is crushed to required granularity respectively, and heavier feeds and light material are added at the two of light material cracking reaction section respectively
Enter in furnace.Lime-ash boiling fluidized reaction section is that biomass carbon remaining in gasifying agent, with lime-ash occurs with superheated steam pure oxygen
Water gas reaction；Heavier feeds cracking reaction section is the combustion gas that combustion gas pure oxygen high temperature burner is come and lime-ash boiling fluidized reaction section
The cracking gas that the water-gas come and this section of reaction generate is fluidized wind；Light material cracking reaction section is this section of superheated steam pure oxygen
The combustion gas and heavier feeds cracking reaction that the next superheated steam pure oxygen gaseous mixture of mixture gas nozzle, combustion gas pure oxygen high temperature burner are come
The cracking gas that section is come and this section of reaction generates is fluidized wind.
The fluid bed heat cracking reaction producer that the present invention uses is divided into fluidisation cracking reaction section, middle fluidisation cracking reaction
Section and lime-ash boiling fluidized reaction section are equipped with bellows in lime-ash boiling fluidized reaction section bottom, and bellows are equipped with superheated steam pure oxygen
Gaseous mixture blast pipe, the gas distribution grid on bellows top are equipped with multiple blast caps, and lime-ash boiling fluidized reaction is slagged tap with having
Device；Two layers of combustion gas pure oxygen high temperature burner is equipped in the middle and lower part of middle fluidisation cracking reaction section；In upper fluidisation cracking reaction pars infrasegmentalis
Mouth is added equipped with heavier feeds, at it to have superheated steam pure oxygen mixture gas nozzle；The upper surface of mouth is added in heavier feeds
Equipped with combustion gas pure oxygen high temperature burner；It more than combustion gas pure oxygen high temperature burner is equipped with light material and mouth is added；In upper cracking fluidized reaction
The middle and upper part of section is equipped with 1-2 layers of superheated steam pure oxygen mixture gas nozzle.
The number of the combustion gas pure oxygen high temperature burner of heat scission reaction producer is by each burner in above two embodiment
The processing materials load of power and furnace determines；Superheated steam provided by superheated steam pure oxygen mixture gas nozzle and pure oxygen be for
Stable reaction in furnace temperature and water vapour needed for water gas reaction is provided.And the characteristic of flammable solid waste such as calorific value, light,
Ratio of heavy material quality etc. determines the position that combustion gas pure oxygen high temperature burner and superheated steam pure oxygen mixture gas nozzle are arranged in furnace
It sets, combustion gas pure oxygen high temperature burner and the position of superheated steam pure oxygen mixture gas nozzle can be interchanged.
Cold shock coil pipe is equipped in the potassium soda metal condensation device, cold shock gas enters coil pipe, low temperature from cold shock gas inlet pipe
Cold shock gas is sprayed from cold shock coil pipe aperture, and for high-temperature fuel gas under the cold shock effect of cold shock gas, high-temperature fuel gas temperature drops to alkali gold
Belong to the boiling point of potassium hereinafter, the alkali metal potassium in high-temperature gas, sodium is made not to separate shape together with net dust bonding with gas phase
At solid-state, it is easily isolated it down, when solidifying to protect back segment waste heat recovery apparatus to bond on it from alkali metal potassium sodium
Caused by damage.Cold shock coil pipe is a round tube, is drilled with equally distributed aperture thereon, there is an adapter tube and the import of cold shock gas thereon
Pipe connects.Cold shock gas can use room temperature combustion gas, can also use saturated vapor or atomization condensed water.
Mouth quantitative continuous is added in light material in the method that the present invention cracks the combustion gas of flammable solid waste with fluid bed heat
The continuous light material being added, due to the high-temp combustion gas, superheated steam pure oxygen gaseous mixture and Pintsch process gas of combustion gas pure oxygen burner
Under the action of carry out cracking reaction rapidly, since the hot conditions and light material of conversion zone are in the sufficiently long reaction of conversion zone
Between, making light material, almost cracking reaction is complete, and only remaining ash content and a small amount of biomass carbon residue send to grey pulp separator；In heavy
The heavier feeds that mouth is quantitatively continuously added to are added in material, under superheated steam pure oxygen gaseous mixture and Pintsch process combustion gas collective effect
Cracking reaction and water gas reaction occur rapidly；Part lighter in product rises with air-flow when heavier feeds crack, with
Light material, which converges, to be continued to crack, and heavier part declines under the effect of gravity, and carries out cracking reaction and water gas reaction, and one
Part is cracked into polymer substance, continues to crack with air-flow rising, and final also into grey pulp separator.In heavier feeds
The material and larger lime-ash of heavier difficult cracking will fall into lime-ash boiling fluidisation section；Lime-ash in grey pulp separator, which is admitted to, send ash
In device, under the action of sending grey high pressure gas inlet pipe high pressure gas, dust sender Ash water pipe, which also send lime-ash to lime-ash to boil, to flow
Change section.Above two high-temperature ash is converged, and passes through boiling fluidisation by the superheated steam pure oxygen gaseous mixture that bottom divides gas blast cap to send
Water gas reaction is carried out with the biomass carbon residue in lime-ash.The water-gas that reaction generates rises the gaseous products with heavier feeds section
Converge uplink.
Flammable solid waste is divided into heavier feeds and light material by the processing of the selection by winnowing in Raw material processing stage, and by two
Kind material is crushed to required granularity respectively, and heavier feeds and light material are added at the two of light material cracking reaction section respectively
Enter in furnace.Lime-ash boiling fluidized reaction section is gasifying agent with superheated steam pure oxygen, makes the remaining biomass carbon in slag that water occur
Coal gas reaction；Middle section fluidisation cracking reaction section is that the combustion gas that combustion gas pure oxygen high temperature burner is come and lime-ash boiling fluidized reaction section are come
Water-gas and this section reaction generate cracking gas be reaction fluidized wind.Upper fluidisation cracking reaction section is combustion gas pure oxygen high temperature burner
The superheated steam pure oxygen gaseous mixture and middle section that the combustion gas come, this section of superheated steam pure oxygen mixture gas nozzle come come and this section is anti-
The cracking gas that should be generated is reaction fluidized wind.
The present invention handles flammable solid waste heat conversion ratio height, and the fuel gases calorific value of production is high；Combustion gas purposes is wide, both may be used
It generates electricity for gas engine, hydrogen energy automobile raw material can also be made, the organic syntheses object such as synthesis ammonia, methanol, dimethyl ether can also be made
Unstripped gas；Lime-ash clinker ignition loss is low in treatment process, without secondary pollution.
Detailed description of the invention
Fig. 1 is structural schematic diagram of the invention；
Fig. 2 is the structural schematic diagram of another embodiment of the present invention；
In figure: 1A is segmentation fluidisation heat scission reaction producer, and 1-1A is light material fluidisation cracking reaction section, and 1B is fluidized bed
Heat scission reaction producer, 1-1B are upper section fluidisation cracking reaction sections, and 1-1-1 is gas outlet pipe, and 1-1-2 is superheated steam
Pure oxygen mixture gas nozzle, 1-1-3 are that mouth is added in light material, and 1-1-4 is combustion gas pure oxygen high temperature burner, and 1-1-5 is heavier feeds
Mouth is added, 1-1-6 is superheated steam pure oxygen mixture gas nozzle, and 1-2A is heavier feeds fluidisation cracking reaction section, and 1-2B is middle section
Cracking reaction section is fluidized, 1-2-1 is combustion gas pure oxygen high temperature burner, and 1-3 is lime-ash boiling fluidized reaction section, and 1-3-1 is a point gas wind
Cap, 1-3-2 are bellows, and 1-3-3 is lime-ash outlet device, and 1-3-4 is pure oxygen superheated steam combi inlet port pipe, and 1-4 is thermometric
Thermocouple, 2 be grey pulp separator, and 2-1 is fuel gas inlet, and 2-2 is gas outlet, and 2-3 is lime-ash outlet, and 3 be dust sender, 3-
1 is to send grey high pressure gas inlet pipe, and 3-2 is dust sender Ash water pipe, and 4 be potassium soda metal condensation device, and 4-1 is fuel gas inlet
Pipe, 4-2 is cold shock gas coil pipe, and 4-3 is cold shock gas inlet pipe, and 4-4 is gas outlet pipe.
Specific embodiment
Below according to the drawings and specific embodiments, the invention will be further described: Fig. 1 is a kind of specific implementation of the present invention
The structural schematic diagram of mode, from fig. 1, it can be seen that by fluidisation heat scission reaction producer, grey pulp separator, dust sender and potassium soda gold
Belong to condenser composition, fluidisation heat scission reaction producer is using segmentation fluidisation heat scission reaction producer 1A, from top to bottom by light
Matter goods fluid cracking reaction section 1-1A, heavier feeds fluidize cracking reaction section 1-2A, lime-ash boiling fluidized reaction section 1-3 group
At.The selection by winnowing in Raw material processing stage is processed, and flammable solid waste is divided into heavier feeds and light material, and by two kinds of materials
It is crushed to required granularity respectively.Segmentation fluidisation heat scission reaction producer 1A reach operating condition under the conditions of, light material and
Mouth is added in the light material of furnace for heavier feeds and heavier feeds are added mouth and are separately added into, in the high-temp combustion of combustion gas pure oxygen burner
It completes to crack by respective approach under the action of the Pintsch process gas generated in gas, superheated steam pure oxygen gaseous mixture and cracking reaction
Reaction.The light material that mouth 1-1-3 is quantitatively adding is added in light material, in combustion gas pure oxygen high temperature burner 1-1-4, superheated steam
Cracking reaction is carried out rapidly under the action of the Pintsch process gas that pure oxygen mixture gas nozzle 1-1-2 and furnace come up below, due to reaction
The hot conditions and light material of section are in the conversion zone sufficiently long reaction time, and making light material, almost cracking reaction is complete, only
Remaining ash content and a small amount of biomass carbon residue send to grey pulp separator 2.The heavy object that mouth 1-1-5 is quantitatively adding is added in heavier feeds
Material, in the Pintsch process combustion gas that superheated steam pure oxygen mixture gas nozzle 1-1-6 and heavier feeds fluidisation cracking reaction section 1-2A come
Cracking reaction and water gas reaction occurs under collective effect rapidly；Part lighter in product is with gas when heavier feeds crack
Stream rises, and converges with light material and continues to crack.Heavier feeds fluidized reaction section 1- is down in heavier part under the effect of gravity
2A, in the high-temperature water gas collective effect that combustion gas and lime-ash boiling fluidisation the section 1-3 of combustion gas pure oxygen high temperature burner 1-2-1 comes
Under, heavier feeds carry out cracking reaction and water gas reaction in furnace 1-2A, and a part is cracked into polymer substance, on air-flow
It rises and continues to crack through light material fluidisation section 1-1A, and it is final also into grey pulp separator 2.It is heavier in heavier feeds section 1-2A
Difficult cracking material and larger lime-ash will fall into lime-ash boiling fluidisation section 1-3.Lime-ash in grey pulp separator 2, which is admitted to, send ash
In device 3, under the action of sending grey high pressure gas inlet pipe 3-1 high pressure gas, dust sender Ash water pipe 3-2 also send lime-ash to ash
Slag boiling fluidisation section 1-3.Above two high-temperature ash is converged, and divides the gas blast cap superheated steam pure oxygen that 1-3-1 is sent to mix by bottom
It closes gas and water gas reaction is carried out with the biomass carbon residue in lime-ash by boiling fluidisation.Lime-ash boiling fluidisation section oxygen and overheat are steamed
The dosage of vapour is calculated by the biomass residual carbon content in two lime-ash.The water-gas that reaction generates rises and heavier feeds section
Gaseous products converge uplink；The lime-ash left after reaction is sent out by lime-ash outlet device 1-3-3.
Fig. 2 is the structural schematic diagram of another specific embodiment of the invention.From fluidized bed Pyrolysis known to attached drawing 2
Producer 1B is answered, cracking reaction section 1-1B is fluidized by upper section from top to bottom, middle section fluidizes cracking reaction section 1-2B, lime-ash boiling stream
Change conversion zone 1-3 composition.Flammable solid waste is divided into heavier feeds and light material.In fluidisation heat scission reaction producer 1B
Under the conditions of reaching operating condition, light material and heavier feeds the light material of fluidisation heat scission reaction producer be added mouth and
Heavier feeds are added mouth and are separately added into, anti-in the high-temp combustion gas of combustion gas pure oxygen burner, superheated steam pure oxygen gaseous mixture and cracking
It answers and completes cracking reaction by respective approach under the action of the Pintsch process gas of generation.Mouth 1-1-3 is added in light material to connect
The continuous light material being quantitatively adding, since the combustion gas pure oxygen high temperature burner 1-1-4 high-temp combustion gas come and superheated steam pure oxygen are mixed
It closes gas jets 1-1-2 and lower section fluidizes the effect for the Pintsch process gas that cracking reaction section is come, ensure that upper section fluidizes cracking reaction
Section 1-1B has the hot conditions of reaction；With suitable air velocity and suitable big reaction compartment come when guaranteeing enough reactions
Between, making light material, almost cracking reaction is complete, and remaining ash content and biomass carbon residue send to grey pulp separator 2.In heavy object
The heavier feeds that mouth 1-1-5 continuous and quantitative is added are added in material, split in superheated steam pure oxygen mixture gas nozzle 1-1-6 and middle section fluidisation
Cracking reaction occurs rapidly under the Pintsch process combustion gas collective effect that solution conversion zone 1-2B comes；Enter the heavier feeds of furnace due to middle section
It fluidizes also rapid under the Pintsch process air-flow and superheated vapour pure oxygen mixture gas nozzle 1-1-6 effect that cracking reaction section 1-2B comes
Cracking reaction and water gas reaction occurs；Part lighter in product rises with air-flow when cracking reaction occurs for heavier feeds, with
Light material, which converges, to be continued to crack.The middle section 1-2B fluidisation cracking reaction section is down in heavier part under the effect of gravity, in combustion gas
Under the high-temperature water gas collective effect that combustion gas and lime-ash boiling the fluidized reaction section 1-3 of pure oxygen high temperature burner 1-2-1 comes, heavy
Material carries out cracking reaction and water gas reaction in furnace, and a part cracking becomes polymer substance, rises with air-flow through upper section
Fluidisation cracking reaction section 1-1B continues to crack, and final also into grey pulp separator 2.In the fluidisation cracking reaction section 1-2B of middle section
Heavier difficult cracking material and larger lime-ash will fall into lime-ash boiling fluidized reaction section 1-3.Lime-ash in grey pulp separator 2
It is admitted in dust sender 3, under the action of sending grey high pressure gas inlet pipe 3-1 high pressure gas, dust sender Ash water pipe 3-2 will be grey
Slag is sent to lime-ash boiling fluidized reaction section 1-3.Above two high-temperature ash is converged, and divides the gas blast cap mistake that 1-3-1 is sent by bottom
Hot steam oxygen mixture carries out water gas reaction with the biomass carbon residue in lime-ash by boiling fluidisation.Lime-ash boiling fluidisation is anti-
The dosage of section superheated steam and oxygen is answered to be calculated by the biomass residual carbon content in two lime-ash.It reacts on the water-gas generated
It rises and converges uplink with the gaseous products of middle section fluidisation cracking reaction；The lime-ash left after reaction passes through lime-ash outlet device 1-3-3
It sends out.High pressure gas can use combustion gas in 3-1, can also use superheated steam.
Potassium soda metal condensation device 4 is equipped with fuel gas inlet pipe 4-1, and cold shock gas enters cold shock disk from cold shock gas inlet pipe 4-3
Pipe 4-2 after low temperature cold shock gas enters coil pipe, is sprayed from cold shock coil pipe aperture, and the high-temperature fuel gas come from fuel gas inlet pipe 4-1 exists
Under the cold shock effect of cold shock gas, temperature drops to the boiling point of alkali metal potassium hereinafter, making the alkali metal potassium in high-temperature gas, sodium condensation simultaneously
Solid-state is formed together with net dust bonding with not separating in gas phase, is easily isolated it down, to protect back segment waste heat to return
It is damaged caused by when receiving unit bonds condensation from alkali metal potassium sodium on it.Cold shock coil pipe 4-2 is a round tube, is drilled with thereon
Equally distributed aperture has an adapter tube to connect with cold shock gas inlet pipe 4-3 on coil pipe.Subsequent combustion gas is flowed from gas outlet pipe 4-4
Out, the heat exchange efficiency and safe operating life of the bonding condensation heat exchanging equipment of alkali metal potassium, sodium on heat exchange equipment are eliminated
Influence.Cold shock gas used in high-temperature fuel gas cold shocking section can be room temperature combustion gas, be also possible to saturated vapor or atomization condensed water.
The T of the temperature thermocouple 1-4 of the fluidisation heat scission reaction producer1-T8With it is corresponding enter furnace gas source switch valve
Interlocked control, makes raw material be in the best Pintsch process state of automatic adjustment in entire burner hearth, and raw material cracking is complete.
Embodiment of the present invention is only the description carried out to the preferred embodiment of invention, not to structure of the present invention
Think and range is defined, under the premise of not departing from invention design philosophy, engineers and technicians are to of the invention in this field
The all variations and modifications that technical solution is made, should all fall into protection scope of the present invention, in the claimed technology of the present invention
Hold, is all described in the claims.
Claims (4)
1. a kind of with the device of fluid bed heat cracking flammable solid waste combustion gas, it is characterised in that: by fluidisation Pyrolysis
Answer producer, grey pulp separator, dust sender and potassium soda metal condensation device composition；The top of the fluidisation heat scission reaction furnace goes out
Mouth is connect with pipeline with grey pulp separator import；The lime-ash outlet of grey pulp separator is connected with dust sender, with dust sender lime-ash
Delivery pipe makes dust sender be connected with boiler ash sediment boiling fluidized reaction section；Grey pulp separator gas outlet pipeline and potassium soda metal
Condenser inlet connection；Potassium soda metal condensation device is additionally provided with cold shock gas inlet pipe and gas outlet pipe；The fluidisation thermal cracking
Reacting producer is segmentation fluidisation heat scission reaction producer or fluid bed heat cracking reaction producer.
2. according to claim 1 with the device of fluid bed heat cracking flammable solid waste combustion gas, it is characterised in that:
The segmentation fluidisation heat scission reaction producer is divided into lime-ash boiling fluidized reaction section, heavier feeds cracking reaction from bottom to top
Section, light material cracking reaction section are equipped with bellows in the lower part of lime-ash boiling fluidized reaction section, and bellows are equipped with pure oxygen superheated steam
The distribution grid of gaseous mixture blast pipe, bellows top is equipped with multiple blast caps, and bottom is to have slag tapping equipment；It is cracked in heavier feeds
Conversion zone middle and lower part is equipped with two layers of combustion gas pure oxygen high temperature burner, and light material cracking reaction pars infrasegmentalis is added equipped with heavier feeds
Mouthful, the lower part that mouth is added in heavier feeds is equipped with superheated steam pure oxygen mixture gas nozzle；The top that mouth is added in heavier feeds is equipped with combustion
Gas pure oxygen high temperature burner, the top of combustion gas pure oxygen high temperature burner are equipped with light material and mouth are added, and crack fluidisation section in light material
Top be equipped with 1-2 layers of superheated steam pure oxygen mixture gas nozzle.
3. according to claim 1 with the device of fluid bed heat cracking flammable solid waste combustion gas, it is characterised in that:
Fluid bed heat cracking reaction producer is divided into fluidisation cracking reaction section, middle fluidisation cracking reaction section and lime-ash boiling fluidized reaction
Section is equipped with bellows in lime-ash boiling fluidized reaction section bottom, and bellows are equipped with superheated steam pure oxygen gaseous mixture blast pipe, bellows top
Gas distribution grid be equipped with multiple blast caps, lime-ash boil fluidized reaction to have slag tapping equipment；In middle fluidisation cracking reaction section
Middle and lower part be equipped with two layers of combustion gas pure oxygen high temperature burner；Heavier feeds are equipped in upper fluidisation cracking reaction pars infrasegmentalis, and mouth is added,
It is to have superheated steam pure oxygen mixture gas nozzle；The upper surface of mouth is added in heavier feeds and is equipped with combustion gas pure oxygen high temperature burner；
It more than combustion gas pure oxygen high temperature burner is equipped with light material and mouth is added；1-2 layers of mistake are equipped in the middle and upper part of upper cracking fluidized reaction section
Hot steam pure oxygen mixture gas nozzle.
4. a kind of with the method for fluid bed heat cracking flammable solid waste combustion gas, it is characterised in that comprise the following processes:
The light material that mouth is quantitatively continuously added to is added in light material, due to high-temp combustion gas, the superheated steam of combustion gas pure oxygen burner
Cracking reaction is carried out rapidly under the action of pure oxygen gaseous mixture and Pintsch process gas, due to the hot conditions and light material of conversion zone
In the conversion zone sufficiently long reaction time, making light material, almost cracking reaction is complete, and only remaining ash content and a small amount of biomass are residual
Carbon sends to grey pulp separator；The heavier feeds that mouth is quantitatively continuously added to are added in heavier feeds, are mixed in superheated steam pure oxygen
Cracking reaction and water gas reaction occur rapidly under gas and Pintsch process combustion gas collective effect；Product when heavier feeds crack
In lighter part rise with air-flow, converge with light material and continue to crack, heavier part declines under the effect of gravity, goes forward side by side
Row cracking reaction and water gas reaction, a part are cracked into polymer substance, continue to crack with air-flow rising, and finally also enter
Grey pulp separator；The material and larger lime-ash of heavier difficult cracking in heavier feeds will fall into lime-ash boiling fluidisation section；
Lime-ash in grey pulp separator is admitted in dust sender, under the action of sending grey high pressure gas inlet pipe high pressure gas, dust sender lime-ash
Delivery pipe, which also send lime-ash to lime-ash to boil, fluidizes section；Above two high-temperature ash is converged, and divides gas blast cap to send by bottom
Superheated steam pure oxygen gaseous mixture carries out water gas reaction with the biomass carbon residue in lime-ash by boiling fluidisation, reacts the water of generation
Coal gas, which rises, converges uplink with the gaseous products of heavier feeds section；Residual ash slag after lime-ash boiling fluidisation section fully reacting
It is sent out by lime-ash outlet device.
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| US5922090A (en) * | 1994-03-10 | 1999-07-13 | Ebara Corporation | Method and apparatus for treating wastes by gasification |
| WO2003002691A1 (en) * | 2001-06-27 | 2003-01-09 | Herhof Umwelttechnik Gmbh | Method and device for the pyrolysis and gasification of material mixtures containing organic components |
| CN101712891A (en) * | 2008-10-07 | 2010-05-26 | 顾鸣海 | Solid fuel combustion and gasification device of fluidized bed or jetting bed with flying ash multiple coal gasification device |
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