CN201058866Y - Entrained flow gasification installation for compressive dry coal powder and under slag draining in solid state - Google Patents
Entrained flow gasification installation for compressive dry coal powder and under slag draining in solid state Download PDFInfo
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- CN201058866Y CN201058866Y CN 200720031839 CN200720031839U CN201058866Y CN 201058866 Y CN201058866 Y CN 201058866Y CN 200720031839 CN200720031839 CN 200720031839 CN 200720031839 U CN200720031839 U CN 200720031839U CN 201058866 Y CN201058866 Y CN 201058866Y
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- entrained flow
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
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Abstract
The utility model relates to a dry pulverized coal pressurized dry-ash entrained flow bed gasification unit, comprising a furnace body and a reaction chamber provided with feed ports, a discharge port and a coal gas outlet, wherein the reaction chamber comprises a first reaction chamber and a second reaction chamber which are arranged from top to the bottom in turn and are communicated with each other; the top of the first reaction chamber is provided with a lower jet feed port; the side wall of the second reaction chamber is provided with more than two horizontal feed ports; the second reaction chamber is communicated with the discharge port and the coal gas outlet. As the utility model adopts a down-flow multi-burner two-stage gasification method, the conversion rate of carbon, the cold coal gas efficiency, the specific coal consumption and the specific oxygen consumption are all higher that the prior gasifier; and the utility model can gasify high ash fusion point coal by adjusting the amount of the feed coal in the second reaction chamber.
Description
Technical field
It is the device of feedstock production synthetic gas that the utility model belongs to the coal, relates in particular to a kind of entrained flow gasification installation for compressive dry coal powder and under slag draining in solid state.
Background technology
The coal gasification reaction is a kind of incomplete oxidation reaction between the vaporized chemical (O2, H2O, CO2) that occurs in carbon and oxygen carrier.Coal Gasification Technology is the basis of process industrials such as the coal-based chemical of development, coal-based liquid fuel, combined cycle generation, polygenerations systeme, hydrogen manufacturing, fuel cell, is common technology, gordian technique and the leading technology of these industries.Can divide three kinds of fixed bed, fluidized-bed and air flow bed by coal in the flow pattern of gasification in the bed.And wherein airflow bed gasification furnace has that single stove processing power is strong, coal adaptability is wide, efficiency of carbon conversion is high and advantage such as Load Regulation is good, has represented the developing direction of Coal Gasification Technology from now on.
Entrained flow gasification is a raw material with fine coal, is entrained into stove by vaporized chemical, and coal and vaporized chemical carry out and flow (piston flow) partial oxidation reaction.For remedying short defective of reaction times, require the stove coal particle size very thin (＜0.1mm) and high temperature of reaction (the flame kernel temperature is more than 2000 ℃), so slag tap is its inevitable outcome.
Entrained flow gasification has dry feed and two kinds of forms of wet method charging.Because refractory lining is adopted in the wet method charging,, require the service temperature can not be above 1400 ℃ for guaranteeing its work-ing life.And dry feed gasification is owing to adopt water wall structure, thus have that adaptability to raw material is wide, cold gas efficiency is high, efficiency of carbon conversion is high, than characteristics such as the oxygen consumption are low, gasification temperature can reach about 1800 ℃.The type of furnace that belongs to the dry feed entrained flow gasification has: the two-stage gasifier of normal pressure K-T stove, Shell, Prenflo, GSP and Xi'an thermal technology institute etc.Normal pressure K-T stove is owing to oxygen, consumption of coal are higher, and along with technical progress, progressively the dry powder stove of pressurized operation replaces.
At present, Holland Shell and German Prenflo vapourizing furnace are the gasification installation with the charging of dry coal powder form, but they have only-the level gasification reaction, in order to allow the molten state lime-ash in the coal gas of high temperature solidify in order to avoid gas cooler is stopped up, have to adopt cooled coal gas a large amount of in the subsequent technique that coal gas of high temperature is carried out chilling, can make coal gas of high temperature be cooled to 900 ℃ by 1400 ℃, its calorific loss is very big, and indexs such as the cold gas efficiency of vapourizing furnace and overall thermal efficiency are all lower.When the gasification high-ash-fusion coal, control gasification temperature thereby SHELL employing interpolation Wingdale reduces the method cause of ash fusion point, and for high ash content, high-ash-fusion coal, it is at a loss what to do then to seem in addition.This mainly is because Shell adopts the cooled coal gas process recycling, after the reduction vapourizing furnace service temperature, and circulation cooled coal gas amount in the time of can controlling the cooled coal gas Quench.If do not add Wingdale, produce more than 100% of tolerance with the cooled coal gas internal circulating load is reached, even reach 150%.Such direct result is that the volume of gas cooler and fly-ash filter is bigger, causes investment higher.And at present Shell and PRENFLO gasification flow process have only pot destroying process, and that this equipment is not only invested is huge, and are not suitable for chemical-process.
And the GSP technology adopts the following spray charging, and the slag-drip opening temperature is temperature minimum point in through gasifier water-cooling wall heat absorption back vaporizer just in time.Must improve the gasification reaction temperature for this reason, thereby guarantee that deslagging is smooth.But not only reduced cold gas efficiency in this case, the while has also increased than the oxygen consumption and has compared coal consumption.And according to coal gasification reaction thermodynamic(al)equilibrium and dynamic analysis, in 1200 ℃～1300 ℃ scopes, coal gasification reaction can carry out fully.
Summary of the invention
The purpose of this utility model is to overcome the shortcoming of prior art, provide a kind of rational in infrastructure, available rate is high and have the entrained flow gasification installation for compressive dry coal powder and under slag draining in solid state of higher carbon transformation efficiency, cold gas efficiency.
For achieving the above object, the technical solution adopted in the utility model is: comprise body of heater and be arranged on the intravital reaction chamber that has opening for feed, discharge port and gas exit of stove, said reaction chamber comprises first reaction chamber that is connected and second reaction chamber that sets gradually from top to bottom, the top of said first reaction chamber is provided with a following spray opening for feed, the sidewall of second reaction chamber is provided with an above horizontal opening for feed, and second reaction chamber also is connected with discharge port and gas exit.
The bottom of first reaction chamber of the present utility model is a tapered configuration, the diameter of second reaction chamber greater than the diameter of first reaction chamber bottom less than the diameter of first reaction chamber; First reaction chamber and second reaction chamber are water wall structure, and this water wall is shell and tube or coil tube type structure; The water wall of first reaction chamber is provided with refractory liner, and the water wall of second reaction chamber is a light-pipe structure; The lower end of second reaction chamber also is provided with the quenched water pipeline that is used for the raw gas that contains solid slag is carried out chilling; Also be provided with water supply and lower collecting box water inlet to first reaction chamber and the second reaction chamber water wall on second reaction chamber, first reaction chamber is provided with and is used to discharge the high-temperature water that water wall produces and the upper header water out of steam.
Because the utility model adopts air-flow downstriker multi-nozzle two stage gasification mode, thereby make efficiency of carbon conversion, cold gas efficiency and than coal consumption, than the oxygen consumption all than existing vapourizing furnace height, and the high-ash-fusion coal that can gasify, only need to adapt to the adjustment second reaction zone coal feeding amount and get final product.
Description of drawings
Fig. 1 is used for the structural representation of chilling process for the utility model;
Fig. 2 is used for the structural representation of pot destroying process for the utility model.
Embodiment
Below in conjunction with drawings and Examples the utility model is described in further detail, but the utility model is not limited to following examples.
The utility model adopts air-flow downstriker multi-nozzle two stage gasification mode.Epimere is first reaction chamber, adopts film water cold wall structure, is laid with refractory liner on the water wall; Hypomere is second reaction chamber, adopts water wall structure, does not lay refractory materials on the water wall, promptly adopts the light pipe formula.First reactor top is provided with a nozzle that sprays into coal dust and vaporized chemical (oxygen and steam), is arranged with two nozzles that spray into coal dust and steam at the second reaction chamber sidewall.Reducing by first reaction chamber links to each other first reaction chamber with second reaction chamber.
Compared with prior art, the utility model is divided into two sections with gasification hearth.At first reaction zone, at top of gasification furnace, 85～95% coals and vaporized chemical spray at this indoor intensive high-temp combustion and gasification reaction of carrying out through nozzle, the gasification reaction temperature is 1400～1800 ℃, reaction mass is about 5 seconds in the residence time of first reaction chamber, in the outlet of first reaction zone, slag enters second reaction zone with the form of liquid state.At second reaction zone, spray into about 5～15% coals and a spot of steam, the coal gas of high temperature that generates with first reaction zone carries out the pyrolysis and the gasification reaction of coal, combustiblecomponents content and calorific value in the coal gas are improved, make the coal gas of high temperature cooling on the other hand, high-temperature fusion attitude lime-ash solidifies, and finally realizes dry ash extraction, reaction mass is 10 seconds in the residence time of second reaction chamber, thereby guarantees efficiency of carbon conversion.
The efficiency of carbon conversion of this vapourizing furnace, cold gas efficiency and than coal consumption, than the oxygen consumption all than existing vapourizing furnace height, and the high-ash-fusion coal that can gasify only needs to adapt to and adjusts the second reaction zone coal feeding amount and get final product.
In chilling process, carry cindery temperature and be and enter the shock chamber after 900～1400 ℃ coal gas passes ring sparger, coal gas is cooled to temperature behind the heat and mass in the shock chamber be 175～350 ℃, enter lower procedure by gas exit, 80% above lime-ash is the separated liquid phase that enters in the shock chamber, discharges from the pulp water outlet then.
In pot destroying process, in the second vaporizer bottom, entrained flow from the regional baffling between the water wall outside and the vapourizing furnace pressure-bearing shell upwards, go out vapourizing furnace then, thereby the flying dust of lime-ash and larger particles is separated with raw gas, the retention efficiency of vapourizing furnace can reach more than 70%, only has a small amount of thin ash to enter the back system.
Claims (6)
1. entrained flow gasification installation for compressive dry coal powder and under slag draining in solid state, comprise body of heater (1) and be arranged on and have an opening for feed (5) in the body of heater (1), the reaction chamber of discharge port (6) and gas exit (8), it is characterized in that: said reaction chamber comprises first reaction chamber (2) that is connected and second reaction chamber (4) that sets gradually from top to bottom, the top of said first reaction chamber (2) is provided with a following spray opening for feed (3), the sidewall of second reaction chamber (4) is provided with (2) individual above horizontal opening for feed (5), and second reaction chamber (4) also is connected with discharge port (6) and gas exit (8).
2. entrained flow gasification installation for compressive dry coal powder and under slag draining in solid state according to claim 1, it is characterized in that: the bottom (7) of said first reaction chamber (2) is a tapered configuration, the diameter of second reaction chamber (4) greater than the diameter of first reaction chamber (2) bottom (7) less than the diameter of first reaction chamber (2).
3. entrained flow gasification installation for compressive dry coal powder and under slag draining in solid state according to claim 1 is characterized in that: said first reaction chamber (2) and second reaction chamber (4) are water wall structure, and this water wall is shell and tube or coil tube type structure.
4. according to claim 1 or 3 described entrained flow gasification installation for compressive dry coal powder and under slag draining in solid state, it is characterized in that: the water wall of said first reaction chamber (2) is provided with refractory liner, and the water wall of second reaction chamber (4) is a light-pipe structure.
5. entrained flow gasification installation for compressive dry coal powder and under slag draining in solid state according to claim 1 is characterized in that: the lower end of said second reaction chamber (4) also is provided with the quenched water pipeline (9) that is used for the raw gas that contains solid slag is carried out chilling.
6. entrained flow gasification installation for compressive dry coal powder and under slag draining in solid state according to claim 1, it is characterized in that: also be provided with water supply and lower collecting box water inlet (10) to first reaction chamber (2) and second reaction chamber (4) water wall on said second reaction chamber (4), first reaction chamber (2) is provided with and is used to discharge the high-temperature water that water wall produces and the upper header water out (11) of steam.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200720031839 CN201058866Y (en) | 2007-05-22 | 2007-05-22 | Entrained flow gasification installation for compressive dry coal powder and under slag draining in solid state |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 200720031839 CN201058866Y (en) | 2007-05-22 | 2007-05-22 | Entrained flow gasification installation for compressive dry coal powder and under slag draining in solid state |
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| CN201058866Y true CN201058866Y (en) | 2008-05-14 |
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| CN 200720031839 Expired - Fee Related CN201058866Y (en) | 2007-05-22 | 2007-05-22 | Entrained flow gasification installation for compressive dry coal powder and under slag draining in solid state |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011009234A1 (en) * | 2009-07-20 | 2011-01-27 | Gu Dadi | Improved gasification process using staged oxygen |
| CN101328434B (en) * | 2008-07-17 | 2011-06-22 | 中国科学技术大学 | Dry coal powder airflow bed gasification furnace |
| CN112725038A (en) * | 2019-10-29 | 2021-04-30 | 中国石油化工股份有限公司 | Coal and petroleum coke co-gasification system and method |
-
2007
- 2007-05-22 CN CN 200720031839 patent/CN201058866Y/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101328434B (en) * | 2008-07-17 | 2011-06-22 | 中国科学技术大学 | Dry coal powder airflow bed gasification furnace |
| WO2011009234A1 (en) * | 2009-07-20 | 2011-01-27 | Gu Dadi | Improved gasification process using staged oxygen |
| CN112725038A (en) * | 2019-10-29 | 2021-04-30 | 中国石油化工股份有限公司 | Coal and petroleum coke co-gasification system and method |
| CN112725038B (en) * | 2019-10-29 | 2021-12-17 | 中国石油化工股份有限公司 | Coal and petroleum coke co-gasification system and method |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080514 Termination date: 20130522 |