CN101050387A - 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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- CN101050387A CN101050387A CN 200710017906 CN200710017906A CN101050387A CN 101050387 A CN101050387 A CN 101050387A CN 200710017906 CN200710017906 CN 200710017906 CN 200710017906 A CN200710017906 A CN 200710017906A CN 101050387 A CN101050387 A CN 101050387A
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- entrained flow
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- 239000003245 coal Substances 0.000 title claims abstract description 39
- 238000002309 gasification Methods 0.000 title claims abstract description 38
- 239000007787 solid Substances 0.000 title claims abstract description 14
- 239000000843 powder Substances 0.000 title claims abstract description 13
- 239000002893 slag Substances 0.000 title claims description 15
- 238000009434 installation Methods 0.000 title claims description 11
- 238000006243 chemical reaction Methods 0.000 claims abstract description 100
- 239000007921 spray Substances 0.000 claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 40
- 239000007789 gas Substances 0.000 abstract description 21
- 238000000034 method Methods 0.000 abstract description 15
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 8
- 229910052799 carbon Inorganic materials 0.000 abstract description 8
- 230000036284 oxygen consumption Effects 0.000 abstract description 5
- 239000000463 material Substances 0.000 abstract 3
- 238000002844 melting Methods 0.000 abstract 1
- 230000008018 melting Effects 0.000 abstract 1
- 239000003034 coal gas Substances 0.000 description 13
- 239000002956 ash Substances 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 239000000126 substance Substances 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 230000035939 shock Effects 0.000 description 3
- 239000002817 coal dust Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 230000004927 fusion Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000006200 vaporizer Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000011819 refractory material Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
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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
干煤粉加压固态排渣气流床气化装置，包括炉体以及设置在炉体内的带有进料口、出料口和煤气出口的反应室，反应室包括自上而下依次设置的相连通的第一反应室和第二反应室，所说的第一反应室的顶部设置有一个下喷式进料口，第二反应室的侧壁上设置有个以上的水平式进料口，第二反应室还与出料口及煤气出口相连通。由于本发明采用气流下行式多喷嘴两段气化方式，从而使碳转化率、冷煤气效率及比煤耗、比氧耗均比现有的气化炉高，而且可以气化高灰熔点煤，只需适应调整第二反应区投煤量即可。
Dry coal powder pressurized solid slagging entrained flow gasification device, including a furnace body and a reaction chamber with a material inlet, a material outlet and a gas outlet arranged in the furnace body. The first reaction chamber and the second reaction chamber are connected, the top of said first reaction chamber is provided with a down-spray feed inlet, and the side wall of the second reaction chamber is provided with a horizontal feed inlet above, The second reaction chamber is also communicated with the material outlet and the gas outlet. Since the present invention adopts the gasification method of multi-nozzle and two-stage downward air flow, the carbon conversion rate, cold gas efficiency, specific coal consumption and specific oxygen consumption are all higher than the existing gasification furnace, and it can gasify coal with high ash melting point, It only needs to adapt to adjust the amount of coal input in the second reaction zone.
Description
Technical field
The invention belongs to the coal is the device of feedstock production synthetic gas, 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 objective of the invention 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 used in the present invention 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 invention 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 present invention 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 present invention;
Fig. 2 is used for the structural representation of pot destroying process for the present invention.
Embodiment
Below in conjunction with drawings and Examples the present invention is described in further detail, but the present invention is not limited to following examples.
The present invention 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 present invention 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.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200710017906 CN101050387A (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 200710017906 CN101050387A (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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| CN101050387A true CN101050387A (en) | 2007-10-10 |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102660329A (en) * | 2012-05-08 | 2012-09-12 | 神华集团有限责任公司 | Two-stage entrained bed solid slagging gasifying device, gasifying method for carbon-containing substance and application of gasifying device |
| CN102965155A (en) * | 2012-11-16 | 2013-03-13 | 中国石油大学(华东) | Liquid slag solid discharging structure of downward entrained-flow bed gasifier |
| CN101665725B (en) * | 2008-09-04 | 2013-04-17 | 中国船舶重工集团公司第七一一研究所 | Composite startup burner for powder coal gasification furnace |
| CN103517968A (en) * | 2011-05-19 | 2014-01-15 | 新日铁住金工程技术株式会社 | Coal gasification system |
| CN103571540A (en) * | 2012-07-19 | 2014-02-12 | 西门子公司 | Waste heat recovery apparatus and method of gasification furnace |
| CN106367118A (en) * | 2016-10-21 | 2017-02-01 | 武汉轻工大学 | Organic solid waste pyrolysis and gasification furnace and steam generation system |
| CN108165312A (en) * | 2018-02-11 | 2018-06-15 | 煤炭科学技术研究院有限公司 | A kind of full water cooling formula fixed bed slag tap gasification installation |
| CN108699456A (en) * | 2015-12-16 | 2018-10-23 | 气体产品与化学公司 | Gasification system and process |
| CN112961704A (en) * | 2021-02-04 | 2021-06-15 | 中国华能集团清洁能源技术研究院有限公司 | Coal gasification cracking gasification furnace |
| CN113549472A (en) * | 2021-08-31 | 2021-10-26 | 宁夏大学 | A novel process and device for treating miscellaneous salts |
| CN113801701A (en) * | 2021-09-06 | 2021-12-17 | 华中科技大学 | Gasification reactor suitable for wide-screening raw materials |
| CN113930260A (en) * | 2021-10-29 | 2022-01-14 | 宁夏神耀科技有限责任公司 | Synthetic gas production device and synthetic gas production method |
-
2007
- 2007-05-22 CN CN 200710017906 patent/CN101050387A/en active Pending
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101665725B (en) * | 2008-09-04 | 2013-04-17 | 中国船舶重工集团公司第七一一研究所 | Composite startup burner for powder coal gasification furnace |
| CN103517968A (en) * | 2011-05-19 | 2014-01-15 | 新日铁住金工程技术株式会社 | Coal gasification system |
| CN102660329B (en) * | 2012-05-08 | 2013-11-20 | 神华集团有限责任公司 | Two-stage entrained bed solid slagging gasifying device, gasifying method for carbon-containing substance and application of gasifying device |
| CN102660329A (en) * | 2012-05-08 | 2012-09-12 | 神华集团有限责任公司 | Two-stage entrained bed solid slagging gasifying device, gasifying method for carbon-containing substance and application of gasifying device |
| CN103571540A (en) * | 2012-07-19 | 2014-02-12 | 西门子公司 | Waste heat recovery apparatus and method of gasification furnace |
| CN102965155A (en) * | 2012-11-16 | 2013-03-13 | 中国石油大学(华东) | Liquid slag solid discharging structure of downward entrained-flow bed gasifier |
| CN108699456A (en) * | 2015-12-16 | 2018-10-23 | 气体产品与化学公司 | Gasification system and process |
| CN106367118A (en) * | 2016-10-21 | 2017-02-01 | 武汉轻工大学 | Organic solid waste pyrolysis and gasification furnace and steam generation system |
| CN106367118B (en) * | 2016-10-21 | 2021-12-07 | 武汉轻工大学 | Organic solid waste pyrolysis gasifier and steam generation system |
| CN108165312A (en) * | 2018-02-11 | 2018-06-15 | 煤炭科学技术研究院有限公司 | A kind of full water cooling formula fixed bed slag tap gasification installation |
| CN112961704A (en) * | 2021-02-04 | 2021-06-15 | 中国华能集团清洁能源技术研究院有限公司 | Coal gasification cracking gasification furnace |
| CN113549472A (en) * | 2021-08-31 | 2021-10-26 | 宁夏大学 | A novel process and device for treating miscellaneous salts |
| CN113801701A (en) * | 2021-09-06 | 2021-12-17 | 华中科技大学 | Gasification reactor suitable for wide-screening raw materials |
| CN113801701B (en) * | 2021-09-06 | 2022-05-20 | 华中科技大学 | A gasification reactor suitable for wide screening of raw materials |
| CN113930260A (en) * | 2021-10-29 | 2022-01-14 | 宁夏神耀科技有限责任公司 | Synthetic gas production device and synthetic gas production method |
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