CN208762459U - A kind of fluid bed powder coal gasification device of flying dust zero-emission - Google Patents
A kind of fluid bed powder coal gasification device of flying dust zero-emission Download PDFInfo
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- CN208762459U CN208762459U CN201821183082.8U CN201821183082U CN208762459U CN 208762459 U CN208762459 U CN 208762459U CN 201821183082 U CN201821183082 U CN 201821183082U CN 208762459 U CN208762459 U CN 208762459U
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Abstract
The utility model discloses a kind of fluid bed powder coal gasification device of flying dust zero-emission, which includes the gasification system by structure compositions such as gasification furnace, high temperature cyclone separator, waste heat boiler, efficient cyclone separator, dedusters and the revert system by structure compositions such as a spin material leg, a rotation material returning device, two spin material legs, two rotation material returning devices, efficient cyclone dipleg, efficient cyclone material returning device, deduster dipleg, deduster material returning device, level-one injector, second level injector, three-level injector, refeed lines.Gasification system and revert system are with the use of directly being all returned to the high temperature center fluerics of gasification furnace for thick flying dust that gas-solid separator under high pressure traps and thin flying dust and maintain temperature and pressure in original gasification furnace constant in the device, realize the zero-emission of flying dust, the effect that in-furnace dust is reunited is improved to greatest extent, production environment is also optimized simultaneously, is that a kind of gasification efficiency is high, can run steadily in the long term, environmental-friendly coal gasifying process.
Description
Technical field
The utility model relates to bed pulverized coal gasification technology fields, and in particular to a kind of fluid bed powder coal gasification of flying dust zero-emission
Device.
Background technique
China is the country of a rich coal, oil starvation, few gas.This energy resource structure background determines that coal is considerably long from now on
Time in will be China's energy main body, be the mainstay of China's economic development.In a variety of Land use systems of coal, coal
The gasification of charcoal is the solid material coal that will be difficult to handle and remove useless component, be converted into be easy to purify and apply
The process of gas.So far, people have developed a variety of reactors, including fixed bed, fluidized bed and entrained-flow reactor
To realize the purpose of Coal Gasification produces combustion gas, synthesis gas.In these reactors, fluidized bed coal gasification reactor is by being had
The ability of the very high heat transfer having and mass-transfer efficiency and a large amount of processing raw material coal particles, has obtained very in coal gasification field
It is widely applied.
In fluidized bed coal gasification reactor, out the effective use of the flying dust of gasification furnace be to ensure that coal gasifier stablize produce gas and
Improve one of the critical issue of efficiency of carbon con version.For a long time, people are typically easy to it is envisioned that being caught using high temperature cyclone separator
Collection flying dust reaches the mesh for improving efficiency of carbon con version and coal gas gas production back to the interior content to reduce carbon residue in flying dust of gasification furnace
's.But on the one hand since the circulating fluid bed reactor bed temperature of normal pressure is relatively low, bed temperature is transported at 800 to 1100 DEG C
Row, and the ash fusion point temperature of most 900 to 1300 DEG C of coal of gasified raw materials, therefore, the circulation fluidized bed coal gasifying technique of normal pressure is difficult
It, can only be another by burning in flying dust feeding boiler to be achieved the purpose that by returning charge to bed by the carbon residue " eating dry squeeze only " in flying dust
It is done to use；Still further aspect, for the fluid bed powder coal gasification furnace reactor of some pressurizations, shared feature is in fluidized bed
There is the central jet pipe of an introducing oxygen in the middle and lower part of gasification furnace, then forms a temperature in the emulsion zone middle and lower part of bed
It spends close to the high temperature center fluerics of ash fusion point temperature, if it is possible to by optimizing revert system for flying dust returning charge to this area
Domain can then be able to achieve the second gasification reaction of carbon residue in flying dust.This relates to the setting of the position of return port and returning charge amount ask
Topic, and so far, very good solution is not yet received in this problem.
Flying dust recycling system relevant to pressurised fluidized bed powder coal gasification furnace is usually by high-temp. vortex in the prior art
Separator and its revert system, dust-extraction unit and its revert system composition.Table one gives the grain of the flying dust of different device trapping
Diameter range and average particle size distribution.Flying dust is smaller by the biggish thick flying dust of average grain diameter and average grain diameter it can be seen from table
Thin flying dust composition, correspond respectively to the flying dust and efficient cyclone and dedusting dress of high temperature cyclone separator (one rotation, two rotation) trapping
Set the flying dust of trapping.
The flying dust size distribution that table one, different device trap
It in conventional pressurised fluidized bed method for pulverized coal gasification or is to be penetrated to thick flying dust back to gasification furnace high temperature center
The attention degree for flowing area is inadequate, as the recycling fly ash granule of Chinese patent CN201010582393.3 method in the return mentioned
The scheme of the flying dust of high temperature center fluerics is only that will be filled during raw gas purifying by efficient cyclone and dedusting in gasification furnace
It sets the thin flying dust trapped and is sent into high temperature center fluerics after pressurization by pneumatic conveying, and under a rotation, two rotation trappings
The thick flying dusts of the overwhelming majority (ratio for accounting for out gasification converter fly ash total amount is higher than 80.0wt%) flowed into naturally by gravity, Huo Zhejian
Single strength is blown into the top of gas distribution grid, and is the periphery of fluidized bed emulsion zone, this part loops back thick winged
Ash is taken away by the ascending air of emulsion zone from the moment for entering gasification furnace, therefore is not reached high temperature center fluerics, as a result
That carbon residue in thick flying dust can not achieve second gasification, ash is not also melted, returning charge again and again to emulsion zone and by
During air-flow is taken away, the flying dust for participating in circulation is cumulative, until the dynamic equilibrium-determined by Cyclone efficiency flies
The ratio between grey internal circulating load and coal input quantity reach 10 times or even 20,30 times, under so high circulating ratio, not only increase high temperature
The abrasion of refeed line under cyclone separator, and abrasion during continuous circulation of thick flying dust becomes thin flying dust, and waste is a large amount of
Energy dropoff high temperature cyclone separator centrifugation, while also the pressure for returning flying dust to high temperature center fluerics being imputed to
Efficient cyclone and dust-extraction unit, this will increase the probability of failure of follow-up equipment such as waste heat boiler or dust-extraction unit；It is exactly
Although it is contemplated that accounting for the thick flying dust returning charge of flying dust overwhelming majority quality ratio to high temperature center fluerics, such as Chinese patent
CN201620741538.2, CN201621065426.6, which are proposed, penetrates the flying dust of the overwhelming majority back to gasification furnace high temperature center
The scheme for flowing area realizes the second gasification reaction of most flying dusts, but still some flying dust for going out gasification furnace is being removed
It is discharged to outside gasification system after the trapping of dirt device, efficiency of carbon con version, gasification efficiency cannot be promoted to greatest extent, due to efficient rotary
The reactivity of wind and the thin flying dust of dust-extraction unit trapping is low, it is also difficult to be effectively utilized.While bringing environmental issue
Also the production cost of coal gas will be improved.
The content of the present invention
The utility model is, gasification furnace relevant device incomplete for flying dust returning charge present in existing method for pulverized coal gasification
What the problems such as high failure rate, proposed.Flying dust zero-emission fluid bed powder coal gasification method and device are intended to provide a kind of adaptability to raw material
By force, easy to operate, stable, method and device that is environmental-friendly, being able to achieve long-term operation.This device can will gasify
The flying dust that journey generates is all returned to high temperature center fluerics and carries out second gasification reaction, realizes that ash is reunited.
To achieve the above object, the fluid bed powder coal gasification device of flying dust zero-emission described in the utility model includes gasification
Furnace, the top of gasification furnace connect the top of level-one high temperature cyclone separator by outlet pipe, level-one high temperature cyclone separator
Top connects the top of second level high temperature cyclone separator, the top exit of second level high temperature cyclone separator and the high temperature of waste heat boiler
Gas entry connection；The lower part coal gas of high temperature outlet of waste heat boiler is connect with the top of efficient cyclone separator, efficient cyclone point
The lower part of top exit connection deduster from device, the top of deduster is equipped with raw gas escape pipe, for raw gas to be discharged；It is high
The lower part for imitating cyclone separator connects the entrance of efficient cyclone material returning device by efficient cyclone dipleg, and efficient cyclone material returning device goes out
Mouth is connected on refeed line；The entrance of the lower part connection deduster material returning device of deduster, the outlet of deduster material returning device is connected to
On refeed line.
In some embodiments, it is equipped with spray sprinkler head at the top of gasification furnace, the lower part of gasification furnace is provided with gasification
Agent distribution grid is provided with nozzle on gasifying agent distribution grid；Gasifying agent distribution grid lower part is equipped with return port；Gasifying agent distribution grid is by gas
Change furnace and be divided into the conversion zone on top and the gasifying agent chamber of lower part, conversion zone side wall be equipped at least one fine coal into
Mouthful, for conveying fine coal；Conversion zone connects the return port, and the side wall of gasifying agent chamber is equipped with gasification agent inlet, gasification
Agent entrance is used to partial gasification agent importing gasifying agent chamber, and enters gasification furnace top by the nozzle on gasifying agent distribution grid
Conversion zone.
In other embodiments, the lower part of the level-one high temperature cyclone separator is returned by one rotation of spin material leg connection
Glassware；The bottom end of one rotation material returning device connects refeed line；One rotation material returning device and refeed line are connected to the entrance of level-one injector together,
The high-temperature oxydation area that the outlet of level-one injector is connected in gasification furnace by the return port.
In other embodiments, the lower part of second level high temperature cyclone separator passes through two spin material legs connection, two rotation returning charge
Device, two rotation material returning devices connect a spin material leg and connect with the entrance of a rotation material returning device.
In other embodiments, second level injector and three-level injector, second level injector are also in series on refeed line
Outlet connect with the entrance of level-one injector, the entrance of second level injector is connect with the outlet of three-level injector, three-level injection
The entrance of device is connect with tracheae is blowed, the entrance connection of the outlet three-level injector of deduster material returning device, efficient cyclone material returning device
Outlet be connected between the outlet of three-level injector and the entrance of second level injector.
Preferably, the deduster is cloth bag or the filter device in addition to cloth bag.
The gasification furnace includes the high-temperature oxydation area that temperature is equal to or higher than the softening temperature of flying dust, the high temperature oxygen
Change area to be located in the high temperature center fluerics.
The bottom of the gasification furnace is equipped with scum pipe, and the outlet of scum pipe is connected to high temperature lag cooler, and scum pipe is used for
The bottom ash in gasification furnace is discharged to high temperature lag cooler, with quantitative discharge lime-ash, it is ensured that the stabilization of bed in gasification furnace.
Nozzle on the gasifying agent distribution grid is for strengthening transverse flow of the bed endoparticle material in addition to axial movement
It is dynamic.
The bottom of the gasification furnace is provided with center oxygen feeding tube, 90% or more oxygen from the center of gasification furnace bottom into
Oxygen pipe enters gasification furnace.
Preferably, it is provided with gravity in a spin material leg and two spin material legs and adjusts flap valve, the level-one high temperature
The gravity adjusting flap valve conduct that cyclone separator and the flying dust of second level high temperature cyclone separator trapping pass through setting in each dipleg
Material returning device, then flying dust is sent into the cone lower part of gasifying agent distribution grid in gasification furnace through level-one injector injection；Efficient cyclone point
Thin flying dust injection is sent into gasifying agent point in gasification furnace using second level injector series connection level-one injector by the thin flying dust from device trapping
The cone lower part of fabric swatch；The thin flying dust of deduster trapping will be thin using three-level injector series connection level-one injector and second level injector
Flying dust injection is sent into the cone lower part of gasifying agent distribution grid in gasification furnace.
Gravity adjusts the material returning device of flap valve form in the operational process of entire gasification furnace, without manual intervention to catching
The flying dust collected carries out returning charge, and the material envelope height by calculating completely realizes that gravity adjusts the automatic opening and closing of flap valve.
The fluid bed powder coal gasification technical process of flying dust zero-emission described in the utility model is as follows:
< 8.0mm is crushed to hereinafter, the fine coal of outer water content < 4.0wt% is sent to gas by coal feed point continuous-stable
Change furnace；The proportion for adjusting vapor and oxidant in gas handling system, so that gasification reaction occurs in gasification furnace for fine coal；
Wherein, the gasification agent inlet below gasifying agent distribution grid is passed through first part's gasifying agent, in gasifying agent vapor with
The proportion of oxidant will ensure that the volume content of oxygen in first part's gasifying agent between 40~70%vol%, adjusts high temperature
The temperature in central jet area occurs oxidation reaction with the carbon in fine coal, generates carbon dioxide or carbon monoxide, and discharging heat will
The granule materials on periphery heat；The effluxvelocity of gas is limited between 40~90m/s in gasification agent inlet, in gasification agent inlet
Continuous bubble phase is formed at upward 0.6~1.2m height, and the material of gasifying agent distribution grid bottom is carried in bubble uphill process
Rise, the material supplement on periphery, so that material forms the interior circulation in emulsion zone；
Then, second part gasifying agent is passed through in gasifying agent distribution grid, it is ensured that the body of oxygen in the second part gasifying agent
Product content is between 5~15vol%；
The raw gas for the entrainment fly ash granule that coal gasification reaction generates passes through before level-one high temperature cyclone separator entrance
Shower water cooling, then sequentially enters level-one high temperature cyclone separator, second level high temperature cyclone separator, waste heat boiler, efficient rotary
Wind separator and deduster are separate raw gas with thick fly ash granule, raw gas is separated with thin fly ash granule, after separation
Thick fly ash granule and thin fly ash granule enter in fluidized-bed gasification furnace below gasifying agent distribution grid, and thereby return to gasification furnace
High temperature center fluerics, the carbon residue in fly ash granule carry out second gasification with gasifying agent and reacts generation coal gas, improve raw gas
Yield, the ash content in particle, which occurs to melt again, poly- is quantitatively discharged gasification furnace by high temperature lag cooler in the form of bottom ash.
The fluid bed powder coal gasification device of flying dust zero-emission described in the utility model compared with prior art, beneficial effect
Be: directly by under high pressure thick flying dust and thin flying dust be all returned to the high temperature center fluerics of gasification furnace, maintain original gas
Change in-furnace temperature and pressure is constant, improve the effect of in-furnace dust reunion to greatest extent, returns to the second gasification of the flying dust come
Further improve efficiency of carbon con version and gas production.The flying dust for being trapped high temperature cyclone separator and deduster by multiple injectors
It is directly recycled into the central high temperature zoneofoxidation of fluidized-bed gasification furnace, ensure that the long-term operation of continuous-stable returning charge and device.
So far, pressurized fluidized bed coal gasifier is difficult to promote the use of major obstacle and is it cannot be guaranteed that coal gas
The stabilization long-term operation of change system.Around this primary and foremost purpose of long-term operation, by with fluidized bed described in the utility model
Method for pulverized coal gasification can guarantee the realization of this target.
The advantages of fluid bed powder coal gasification device of flying dust zero-emission described in the utility model and effect are as follows:
1. ultralow circulating ratio participates in the ratio between flying dust and coal input quantity of circulation, is commonly referred to as circulating ratio, the value is by routine
As many as 10 times or even 20,30 times under pressurised fluidized bed, it is reduced to 1 times or lower.Circulating ratio reduction can effectively improve carbon
Conversion ratio and gasification efficiency provide most important premise for the long-term operation of follow-up equipment.
2. multiple oxygen feeding tubes at gasifying agent distribution grid center can make oxidant jet-stream wind in a manner of cross one another into oxygen,
The high temperature center fluerics in coal gasifier is expanded, the contact area of gasifying agent and feed coal is increased, accelerates reaction rate, mention
High gasification efficiency and efficiency of carbon con version.
3. flying dust is sent into high temperature center fluerics plus after two diplegs merging by two high temperature cyclone separator series connection, really
It protects cyclone dust removal efficiency and is higher than 99% or more, secondary take out of of flying dust is reduced to 2g/Nm3Hereinafter, fundamentally solving downstream
The problem of equipment abrasion.
4. efficient cyclone separator and deduster are arranged after waste heat boiler, the flying dust in raw gas is further decreased
Content makes the dustiness in coal gas reach the dustiness requirement of industrial combustion gas (fields such as alumina roasting furnace).Efficient cyclone point
From the thin flying dust (carbon content therein is between 60~80wt%) under device and deduster trapping, trapped with high temperature cyclone separator
Under thick flying dust together pass through revert system return gasification furnace high temperature center fluerics carry out second gasification reaction.Improve carbon conversion
The zero-emission of flying dust is realized while rate, cold gas efficiency.
5. the exhaust system for the bottom slag that gasifies uses high temperature lag cooler, high temperature bottom slag directly passes through high temperature lag cooler and quantitatively arranges
It puts, ensure that the stabilization of bed height in gasification furnace and recycles the heat in lime-ash, improve the gasification furnace entirety thermal efficiency.
6. spray cooling is arranged before high temperature cyclone separator import, the temperature of gasifier gas out can be stablized, this sets
The advantages of setting is to stablize the operation of cyclone separator, prevents from burning out follow-up equipment, such as waste heat boiler, gas-pipe line, significantly
The probability of failure for reducing follow-up equipment guarantees the long-period stable operation of system.
7. the distribution of oxidant and vapor ratio at coal gasifier gasifying agent distribution grid and gasification agent inlet, it is ensured that gasification
The concentration of oxygen concentration of oxygen in 40~70vol%, gasifying agent distribution grid gasifying agent is not higher than in gasifying agent in agent entrance
15.0vol%.While having the advantage that the high gasification efficiency of guarantee in this way, it is not easy slagging on distribution grid and causes unplanned
Property parking maintenance.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the fluid bed powder coal gasification device of flying dust zero-emission described in the utility model.
Specific embodiment
The following examples illustrate the utility model, but is not intended to limit the scope of the present invention.
As shown in Figure 1, the fluid bed powder coal gasification device of flying dust zero-emission described in the utility model includes gasification furnace 1,
It is equipped with spray sprinkler head 6 at the top of gasification furnace 1, the lower part of gasification furnace 1 is provided with gasifying agent distribution grid 3, gasifying agent distribution grid 3
On be provided with nozzle；Gasifying agent distribution grid lower part is equipped with return port 4；Gasification furnace 1 is divided into the anti-of top by gasifying agent distribution grid 3
The gasifying agent chamber of region and lower part is answered, conversion zone side wall is equipped at least one fine coal import, for conveying fine coal；Reaction
Region connects the return port, and the side wall of gasifying agent chamber is equipped with gasification agent inlet, and gasification agent inlet is used for partial gasification
Agent imports gasifying agent chamber, and enters the conversion zone on 1 top of gasification furnace by the nozzle on gasifying agent distribution grid 3；Gasification furnace 1
Top the top of level-one high temperature cyclone separator 8 is connected by outlet pipe 7, the lower part of level-one high temperature cyclone separator 8 is logical
Cross one rotation material returning device 18 of a spin material leg 21 connection；The bottom end of one rotation material returning device 18 connects refeed line 23；One revolves material returning device 18 and returns
Expects pipe 23 is connected to the entrance of level-one injector 19 together, and the outlet of level-one injector 19 is connected to gasification by the return port
High temperature center fluerics 2 in furnace；The top of the top connection second level high temperature cyclone separator 9 of level-one high temperature cyclone separator 8,
The top exit of second level high temperature cyclone separator 9 is connect with the coal gas of high temperature entrance of waste heat boiler 10；The separation of second level high-temp. vortex
By two spin material legs 22 connection, two rotation material returning device 17, two rotation material returning devices 17 connect a spin material leg 21 and return with a rotation for the lower part of device 9
The entrance of glassware 18 connects；The lower part coal gas of high temperature outlet of waste heat boiler 10 is connect with the top of efficient cyclone separator 11, high
The lower part of the top exit connection deduster 12 of cyclone separator 11 is imitated, the top of deduster 12 is equipped with raw gas escape pipe, uses
In discharge raw gas；The lower part of efficient cyclone separator 11 connects entering for efficient cyclone material returning device 14 by efficient cyclone dipleg 24
Mouthful, the outlet of efficient cyclone material returning device 14 is connected on refeed line 23；The lower part of deduster 12 is connected by deduster dipleg 25
The entrance of deduster material returning device 13, the outlet of deduster material returning device 13 are connected on refeed line 23；It is also in series on refeed line 23
The outlet of second level injector 16 and three-level injector 15, second level injector 16 is connect with the entrance of level-one injector 19, and second level is drawn
The entrance of emitter 16 is connect with the outlet of three-level injector 15, and the entrance of three-level injector 15 is connect with tracheae is blowed, deduster
The entrance of the outlet three-level injector 15 of material returning device 13 connects, and the outlet of efficient cyclone material returning device 14 is connected to three-level injector 15
Outlet and second level injector 16 entrance between.
Preferably, the deduster 12 is cloth bag or other filter devices.
The gasification furnace includes the high-temperature oxydation area that temperature is equal to or higher than the softening temperature of flying dust, the high temperature oxygen
Change area to be located at 2 in the high temperature center fluerics.
The bottom of the gasification furnace 1 is equipped with scum pipe 5, and the outlet of scum pipe 5 is connected to high temperature lag cooler 20, scum pipe
5 bottom ash for being discharged in gasification furnace 1 is to high temperature lag cooler 20, with quantitative discharge lime-ash, it is ensured that bed is steady in gasification furnace 1
It is fixed.
Nozzle on the gasifying agent distribution grid 3 is for strengthening transverse flow of the bed endoparticle material in addition to axial movement
It is dynamic.
The bottom of the gasification furnace is provided with center oxygen feeding tube, 90% or more oxygen from the center of gasification furnace bottom into
Oxygen pipe enters gasification furnace.
Preferably, it is provided with gravity in a spin material leg 21 and two spin material legs 22 and adjusts flap valve, the level-one
The gravity adjusting flap valve that high temperature cyclone separator and the flying dust of second level high temperature cyclone separator trapping pass through setting in each dipleg
As material returning device, then flying dust is sent into the cone lower part of gasifying agent distribution grid in gasification furnace through 19 injection of level-one injector；Efficiently
The thin flying dust of cyclone separator trapping connects level-one injector using second level injector 16 will be in thin flying dust injection feeding gasification furnace
The cone lower part of gasifying agent distribution grid；The thin flying dust of deduster trapping is drawn using three-level injector series connection level-one injector and second level
Thin flying dust injection is sent into the cone lower part of gasifying agent distribution grid in gasification furnace by emitter.
Gravity adjusts the material returning device of flap valve form in the operational process of entire gasification furnace, without manual intervention to catching
The flying dust collected carries out returning charge.Although the gravity, which adjusts flap valve, belongs to " mechanical valve " scope, without providing any required people
For the mechanism of adjusting, the material envelope height by calculating completely realizes that gravity adjusts the automatic opening and closing of flap valve, really real
Show intelligent unattended, and entire revert system is in a kind of " stable equilibrium " operating status.
The fluid bed powder coal gasification technical process of flying dust zero-emission described in the utility model is as follows:
< 8.0mm is crushed to hereinafter, the fine coal of outer water content < 4.0wt% is sent to gas by coal feed point continuous-stable
Change furnace；The proportion for adjusting vapor and oxidant in gas handling system, so that gasification reaction, fine coal occur in gasification furnace for fine coal
The raw gas for the entrainment fly ash granule that gasification reaction generates is cooled down before level-one high temperature cyclone separator entrance by shower water, and
After sequentially enter level-one high temperature cyclone separator, second level high temperature cyclone separator, waste heat boiler, efficient cyclone separator and dedusting
Device is separate raw gas with thick fly ash granule, raw gas is separated with thin fly ash granule, the thick fly ash granule after separation with
Thin fly ash granule enters in fluidized-bed gasification furnace below gasifying agent distribution grid, and thereby returns to gasification furnace high temperature center jet stream
Area, the carbon residue in fly ash granule carry out second gasification with gasifying agent and reacts generation coal gas, improve the yield of raw gas, in particle
Ash content occur to melt again and poly- gasification furnace be quantitatively discharged by high temperature lag cooler in the form of bottom ash.
Several important control technology parameters are as follows in gasification process described in the utility model:
Preferably, the gasification agent inlet below gasifying agent distribution grid is passed through first part's gasifying agent, water steams in gasifying agent
The proportion of gas and oxidant will ensure that the volume content of oxygen in first part's gasifying agent between 40~70%vol%, is adjusted
The temperature of high temperature center fluerics occurs oxidation reaction with the carbon in fine coal, generates carbon dioxide or carbon monoxide, and discharge heat
Amount heats the granule materials on periphery；The effluxvelocity of gas is limited between 50~80m/s in gasification agent inlet, in gasifying agent
Continuous bubble phase is formed at the upward 0.6~1.2m height of entrance, carries gasifying agent distribution grid bottom in bubble uphill process
Material rises, the material supplement on periphery, so that material forms very important interior circulation in emulsion zone.
Then, second part gasifying agent is passed through in gasifying agent distribution grid, it is ensured that the body of oxygen in the second part gasifying agent
Product content is between 5~15vol%.
The utility model is considered after fully entering high temperature center fluerics due to fly ash granule zero-emission, residual in flying dust
The burning of carbon can further increase the temperature of emulsion zone in gasification furnace.To prevent because the excessive of the ash content that high temperature may cause melts
Melt, and the deslagging blockage that thus may cause, the generation of full emulsion zone bed sintering phenomenon, for gasifying agent distribution grid
Percent opening and gasifying agent distribution grid on the spouted direction of each gas nozzle corresponding adjustment has also been made, compared to conventional pressurization
Fluidized bed, gas distribution grid percent opening reduce 50~60%, and gas nozzle is adjusted to horizontal direction by 45 ° in original horizontal direction
Lower 15 °, main purpose is to strengthen lateral flow of the bed endoparticle material in addition to axial movement, this will substantially reduce high temperature institute
Cause the probability that part remains in a standstill, is sintered.
The utility model is as follows to the adjustment of the distribution of oxygen, i.e., 90% or more oxygen from the center of gasification furnace bottom into
Oxygen pipe enters, this is not exclusively advantageous for the stroke of high temperature center fluerics, is also beneficial to improve the gasified reverse in entire gasification furnace
Temperature is answered, so that the cost of effective gas is improved to greatest extent in coal gas.
Test shows in one embodiment, and the method for the utility model can will be almost all of in gasification reaction coal
Carbon conversion is coal gas, and efficiency of carbon con version is elevated above 99% from lower than 95% for the coal of different gasification reactivities,
Almost all of flying dust is discharged from fluidized-bed reactor in the form of the bottom slag that gasifies.
For test the utility model process effect, carried out control experiment, wherein comparative experiments one is only thin
Flying dust returns to high temperature center fluerics；Comparative experiments two is that thick flying dust is returned to high temperature center fluerics, and thin flying dust is not sent back to
Into gasification furnace 1.Other conditions remain unchanged in three experiments, using coal, oxygen-enriched (80.0vol%) and steam.Gasification
Pressure in furnace is 600kPa, and temperature is about 1040~1050 DEG C.For fly ash carry to gasification furnace 1 to be blowed gas as dirty nitrogen
(95.0vol%).
As shown in Table 2, which belongs to the lower coal of gasification reactivity for the coal analysis report of the feed coal used
Kind.
Table two, the feed coal composition into gasification furnace
| Ingredient, wt% | Numerical value |
| Carbon | 56.65 |
| Hydrogen | 3.15 |
| Oxygen | 12.91 |
| Nitrogen | 1.03 |
| Sulphur | 0.81 |
| Ash content | 15.44 |
| Moisture | 10.00 |
The test result of the utility model gasification process is listed in table three compared with comparative experiments.
Table three, efficiency of carbon con version, cold gas efficiency
The raising of efficiency of carbon con version in this field be it is relatively difficult to achieve, as can be seen from the above data, the utility model gasification
Method is substantially better than comparative experiments one and two in terms of efficiency of carbon con version and cold gas efficiency.The outer of no flying dust is realized in environmental protection
Row, the probability of non-normal stop caused by reducing equipment due to abrasion.
Although above having made detailed description to the utility model with generality explanation and specific embodiment,
On the basis of the utility model, it can be made some modifications or improvements, this is apparent to those skilled in the art
's.Therefore, these modifications or improvements on the basis of without departing from the spirit of the present invention, belong to the utility model and want
Seek the range of protection.
Claims (9)
1. a kind of fluid bed powder coal gasification device of flying dust zero-emission, which is characterized in that the fluidized bed of the flying dust zero-emission
Gasifying powder coal device includes gasification furnace, and the top of gasification furnace connects the top of level-one high temperature cyclone separator by outlet pipe,
The top of the top connection second level high temperature cyclone separator of level-one high temperature cyclone separator, the top of second level high temperature cyclone separator
Outlet is connect with the coal gas of high temperature entrance of waste heat boiler；The outlet of lower part coal gas of high temperature and the efficient cyclone separator of waste heat boiler
Top connection, the lower part of the top exit connection deduster of efficient cyclone separator, the top of deduster is equipped with raw gas outlet
Pipe, for raw gas to be discharged；The lower part of efficient cyclone separator connects entering for efficient cyclone material returning device by efficient cyclone dipleg
Mouthful, the outlet of efficient cyclone material returning device is connected on refeed line；The entrance of the lower part connection deduster material returning device of deduster, dedusting
The outlet of device material returning device is connected on refeed line.
2. the fluid bed powder coal gasification device of flying dust zero-emission as described in claim 1, which is characterized in that on the top of gasification furnace
Portion is equipped with spray sprinkler head, and the lower part of gasification furnace is provided with gasifying agent distribution grid, is provided with nozzle on gasifying agent distribution grid；Gasification
Agent distribution grid lower part is equipped with return port；Gasification furnace is divided into the conversion zone on top and the gasifying agent of lower part by gasifying agent distribution grid
Chamber, conversion zone side wall is equipped at least one fine coal import, for conveying fine coal；Conversion zone connects the return port,
The side wall of gasifying agent chamber is equipped with gasification agent inlet, and gasification agent inlet is used to partial gasification agent importing gasifying agent chamber, and
Enter the conversion zone on gasification furnace top by the nozzle on gasifying agent distribution grid.
3. the fluid bed powder coal gasification device of flying dust zero-emission as claimed in claim 2, which is characterized in that the level-one high temperature
The lower part of cyclone separator passes through one rotation material returning device of spin material leg connection；The bottom end of one rotation material returning device connects refeed line；One rotation is returned
Glassware and refeed line are connected to the entrance of level-one injector together, and the outlet of level-one injector is by the return port by return
Material is sent to the high-temperature oxydation area in gasification furnace.
4. the fluid bed powder coal gasification device of flying dust zero-emission as claimed in claim 3, which is characterized in that second level high-temp. vortex
The lower part of separator passes through two spin material legs connection, two rotation material returning devices, and two rotation material returning devices connect a spin material legs and revolve material returning device with one
Entrance connection.
5. the fluid bed powder coal gasification device of flying dust zero-emission as described in claim 1, which is characterized in that also gone here and there on refeed line
It is associated with second level injector and three-level injector, the outlet of second level injector is connect with the entrance of level-one injector, second level injector
Entrance connect with the outlet of three-level injector, the entrance of three-level injector is connect with tracheae is blowed, the material returning device under deduster
Outlet is connect with three-level injector entrance, and the outlet of efficient cyclone material returning device is connected to the outlet of three-level injector and second level injector enters
Between mouthful.
6. the fluid bed powder coal gasification device of flying dust zero-emission as described in any one in claim 1-5, which is characterized in that described
Deduster be cloth bag or the filter device in addition to cloth bag.
7. the fluid bed powder coal gasification device of flying dust zero-emission as described in any one in claim 1-5, which is characterized in that described
The bottom of gasification furnace be provided with center oxygen feeding tube, 90% or more oxygen enters gasification from the center oxygen feeding tube of gasification furnace bottom
Furnace；The bottom of the gasification furnace is equipped with scum pipe, and the outlet of scum pipe is connected to high temperature lag cooler, and scum pipe is for being discharged gas
Change the bottom ash in furnace to high temperature lag cooler, with quantitative discharge lime-ash, it is ensured that the stabilization of bed in gasification furnace.
8. the fluid bed powder coal gasification device of flying dust zero-emission as described in any one in claim 1-5, which is characterized in that described
Gasification furnace include temperature be equal to or higher than flying dust softening temperature high temperature center fluerics, the high-temperature oxydation area is located at
In the high temperature center fluerics.
9. the fluid bed powder coal gasification device of flying dust zero-emission as claimed in claim 4, which is characterized in that a rotation material
It is provided with gravity in leg and two spin material legs and adjusts flap valve, the level-one high temperature cyclone separator and the separation of second level high-temp. vortex
The flying dust of device trapping adjusts flap valve as material returning device by the gravity being arranged in each dipleg, and then flying dust draws through level-one injector
Penetrate the cone lower part for being sent into gasifying agent distribution grid in gasification furnace；The thin flying dust of efficient cyclone separator trapping utilizes second level injector
Thin flying dust injection is sent into the cone lower part of gasifying agent distribution grid in gasification furnace by level-one injector of connecting；The thin of deduster trapping flies
Thin flying dust injection is sent into gasifying agent in gasification furnace using three-level injector series connection level-one injector and second level injector and is distributed by ash
The cone lower part of plate.
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| CN201821183082.8U CN208762459U (en) | 2018-07-25 | 2018-07-25 | A kind of fluid bed powder coal gasification device of flying dust zero-emission |
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| CN201821183082.8U CN208762459U (en) | 2018-07-25 | 2018-07-25 | A kind of fluid bed powder coal gasification device of flying dust zero-emission |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108753367A (en) * | 2018-07-25 | 2018-11-06 | 上海正申建设工程有限公司 | A kind of the fluid bed powder coal gasification device and technique of flying dust zero-emission |
| CN110484301A (en) * | 2019-08-30 | 2019-11-22 | 哈尔滨工业大学 | A kind of grace classification gasification system of flying dust dry-type clean processing |
| CN110701607A (en) * | 2019-11-14 | 2020-01-17 | 山东福宽生物工程有限公司 | Boiler fly ash reburning device and method |
-
2018
- 2018-07-25 CN CN201821183082.8U patent/CN208762459U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108753367A (en) * | 2018-07-25 | 2018-11-06 | 上海正申建设工程有限公司 | A kind of the fluid bed powder coal gasification device and technique of flying dust zero-emission |
| CN110484301A (en) * | 2019-08-30 | 2019-11-22 | 哈尔滨工业大学 | A kind of grace classification gasification system of flying dust dry-type clean processing |
| CN110701607A (en) * | 2019-11-14 | 2020-01-17 | 山东福宽生物工程有限公司 | Boiler fly ash reburning device and method |
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