CN102277200A - Method for preparing coal gas by virtue of pulverized coal grading gasification - Google Patents
Method for preparing coal gas by virtue of pulverized coal grading gasification Download PDFInfo
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- CN102277200A CN102277200A CN2011101857687A CN201110185768A CN102277200A CN 102277200 A CN102277200 A CN 102277200A CN 2011101857687 A CN2011101857687 A CN 2011101857687A CN 201110185768 A CN201110185768 A CN 201110185768A CN 102277200 A CN102277200 A CN 102277200A
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- fluidized bed
- gasification
- coal gas
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- 238000002309 gasification Methods 0.000 title claims abstract description 38
- 239000003245 coal Substances 0.000 title claims abstract description 34
- 239000003034 coal gas Substances 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims abstract description 17
- 239000002245 particle Substances 0.000 claims abstract description 20
- 239000000463 material Substances 0.000 claims abstract description 13
- 239000007787 solid Substances 0.000 claims abstract description 10
- 238000002156 mixing Methods 0.000 claims abstract description 9
- 238000007599 discharging Methods 0.000 claims abstract description 5
- 238000000197 pyrolysis Methods 0.000 claims abstract description 4
- 239000002893 slag Substances 0.000 claims description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 239000002817 coal dust Substances 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 6
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- 239000010419 fine particle Substances 0.000 claims description 5
- 238000004062 sedimentation Methods 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 11
- KSSNXJHPEFVKHY-UHFFFAOYSA-N phenol;hydrate Chemical compound O.OC1=CC=CC=C1 KSSNXJHPEFVKHY-UHFFFAOYSA-N 0.000 abstract description 4
- 230000001105 regulatory effect Effects 0.000 abstract 1
- 238000003911 water pollution Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 30
- 239000002956 ash Substances 0.000 description 21
- 238000005516 engineering process Methods 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 239000000126 substance Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000010883 coal ash Substances 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 238000005336 cracking Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000036284 oxygen consumption Effects 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 206010012735 Diarrhoea Diseases 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 206010047700 Vomiting Diseases 0.000 description 1
- PIYVNGWKHNMMAU-UHFFFAOYSA-N [O].O Chemical compound [O].O PIYVNGWKHNMMAU-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 239000011362 coarse particle Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 235000003599 food sweetener Nutrition 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 230000002000 scavenging effect Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000003765 sweetening agent Substances 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 230000008673 vomiting Effects 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention relates to a method for preparing coal gas by virtue of pulverized coal grading gasification, and the method comprises the following steps: mixing pulverized coal entering a furnace, quickly-fluidified high-temperature particles and gasified gas in a fluidized bed; causing medium and small particles to flow upwards; carrying out pyrolysis at high temperature of 900-1000DEG C; separating in a cyclone separator via a gas-solid mixing pipeline; returning medium particles back to the lower part of the main body of a circulating fluidized bed via a first-stage material returning device; discharging coal gas carried with small particles from the upper port of the cyclone separator; entering a superheated steam heat exchanger for exchanging heat and separating via a high-temperature coal gas pipeline; then, entering a circulation separator; and discharging the coal gas from a user coal gas outlet. The method has the characteristics that the circulating fluidized bed and the entrained flow bed are integrated to bring high gasification intensity, flexibly regulated production load, stable and reliable operation, high operation rate and the like, the coal gas production cost is lowered, and no phenol water pollution is generated.
Description
Technical field
The invention belongs to the gasification of coal field, particularly relate to the method that a kind of fine coal classification gasification is produced coal gas.
Background technology
At present, Coal Gasification Technology mainly is divided into by gasification mode both at home and abroad: fixed bed lump coal gasification technology; Fluidized bed pulverized coal gasification technology; Entrained flow bed gasification technology.
Fixed bed (moving-bed) Coal Gasification Technology is the gas making of lump coal air vapor.Its advantage: be that technology maturation, facility investment are few, especially the intermittent type static bed coal gasification does not need pure oxygen, just can obtain the synthetic gas of nonnitrogenous gas with water vapour and air gas making.Its shortcoming: carbon residue content height (10%～30%) in the coal ash, the coal restriction is tight, gasification high-quality lump coal, cause many enterprises expense of raw materials height, production cost is high, its type of furnace mainly contains single hop stove (GEGas, Shandong are strange, MERC etc.), two sections stoves (ATC/Wellman, FW-stoic, Rule-100) of dry method ash discharge, the slag tap fixed-bed gasification furnace (BGG/Lurgi, GFETC) of dry method ash discharge, and producing phenol water has pollution.
The fluid bed powder coal gasification technology is to be raw material with fine coal, is the continuous gas making of vaporized chemical with oxygen water vapour.Its advantage: directly with cheap various fine coal make raw material, the gas production ability is moderate, gasification efficiency is high, low in the pollution of the environment, the gas production cost is low.Its shortcoming: facility investment is higher, the flying dust amount is big and carbon residue content height (20%～30%), coal ash in carbon residue content higher (5～15%), the difficult problem of suffering from vomiting and diarrhoea is promptly arranged.The main type of furnace has Wen Keer vapourizing furnace, high temperature Wen Keer vapourizing furnace, CO
2Receptor gasification, U-Gas ash fusing fluidized bed, western room fluidized-bed gasification, Shanxi coalification institute of the Chinese Academy of Sciences are ash fusing fluidized bed etc.
The air-flow bed coal-gasification technology is that fines is a raw material, is the continuous gas making of vaporized chemical with oxygen water vapour, slag tap.Its advantage is that carbon residue content higher (2～7%) in gas production ability height, gasification efficiency height, low in the pollution of the environment, the coal ash, gas production cost are low.Its shortcoming is: facility investment height, fineness of pulverized coal require high, pulverize the energy consumption height; Temperature of reaction height (about 1400 ℃) time short (several seconds) but charging coal dust can not preheatings, and the oxygen consumption is big, and energy utilizes unreasonable, coal water slurry charging oxygen consumption height especially, and the carbon effective rate of utilization is lower.The type of furnace mainly contains K-T gasification, Texaco's coal gasification process, and two sections entrained flow gasification methods are domestic still in research.
The requirement that these coal gasification methods are different according to the user, adopt different vaporized chemical (as air-water vapour, oxygen-water vapor, oxygen enrichment-water vapour) can produce the coal gas of different calorific values and component, the coal gas that acts as a fuel, synthetic gas and reducing gas and hydrogen or combined cycle generation.
Summary of the invention
Purpose of the present invention is at the shortcoming of above-mentioned prior art, it is one that a kind of circulating fluidized bed and air flow bed are provided, gasification intensity is big, the production Load Regulation is flexible, stable and reliable operation, operation factor height, reduce the gas production cost, the fine coal classification gasification that does not produce the pollution of phenol water is produced the method for coal gas.
For this purpose, the present invention adopts following technical scheme:
The fine coal classification gasification is produced the method for coal gas, the steps include: that coal charge sends in the center lumen of circulating fluidized bed main body by coal filling hole, superheated vapour from the superheated vapour interchanger, enter the air mixed of mixing tank and gas blower by the superheated vapour pipeline, enter circulating fluidized bed from the sparger of circulating fluidized bed bottom part body, go into the stove coal dust in fluidized-bed with fast fluidizing high-temperature particle and the blending of gasification gas, the small particles coal dust upwards flows, high temperature 900-1000 ℃ pyrolysis, entering cyclonic separator through the gas-solid mixed pipe line separates, middle particle returns the circulating fluidized bed lower body part through the one-level material returning device, coal gas carries small-particle and comes out from cyclonic separator is suitable for reading, enter the superheated vapour interchanger through the coal gas of high temperature pipeline and carry out heat exchange and separation, enter the circulation separator again, coal gas is from discharging for user's gas exit, the fine particle that the isolating small particles of superheated vapour interchanger is separated through sedimentation pipeline and circulation separator enters the air flow bed reactor by the secondary material returning device, the air of gas blower enters the air flow bed reactor for oxidation reactions through the air arm, the fine particle of separating enters the air flow bed reactor through the secondary material returning device, reaction back liquid slag enters the interior bottom of circulating fluidized bed main body mixes as heat of gasification with the solid ash, and low carbon containing lime-ash is arranged in airtight ash bucket via heat exchange type spiral ash ejector.
The characteristics that the present invention has are: 1, an equipment has circulating fluidized bed and air flow bed two portions simultaneously, and its circulating fluidized bed and air flow bed are one, have realized the coal grading gasification; 2, gasification intensity is big, and equipment volume is little, and steel consumption is low, and fixed investment reduces greatly; 3, simple to operate, the start-stop car is convenient, and the production Load Regulation is flexible, and continuity is good, and coal adaptability is strong; 4, carry semicoke secretly and enter different beds, stable and reliable operation, operation factor height by the fractional separation device being set, making by the difference of granularity; 5, be vaporized chemical with air and steam only, methane content is just very high in the coal gas, and the caloric power of gas height is substantially free of tar; 6, can utilize cheap brown coal and lower-grade metamorphic bituminous acting as a fuel, reduce the gas production cost; 7, partial desulfurization in the realization response device has been simplified scavenging process, and it is pollution-free not produce phenol water, and 8, the High Temperature Gas and the liquid lime-ash that generate in the air flow bed be the circulating fluidized bed heat supply simultaneously, liquid lime-ash is converted into the solid lime-ash and discharges, and the ash discharge process is simple.
Description of drawings
Accompanying drawing: process flow diagram of the present invention.
Number in the figure: 1. circulating fluidized bed main body, 2, gas-solid mixed pipe line, 3. cyclonic separator, 4. coal filling hole, 5. sparger, 6. heat exchange type spiral ash ejector, 7. one-level material returning device, 8. gas blower, 9, mixing tank, 10., the air arm, 11 air flow bed reactors, 12. secondary material returning devices, 13. superheated vapour pipelines, 14, sedimentation pipeline, 15, the circulation separator, 16, the superheated vapour interchanger, 17, middle temperature gaspipe line, 18, for the user gas exit, 19, the coal gas of high temperature pipeline.
Embodiment
Coal charge less than additives such as the qualified fine coal of 10mm and a spot of Wingdales is sent in the center lumen of circulating fluidized bed main body 1 by coal filling hole 4, superheated vapour from superheated vapour interchanger 16, enter mixing tank 9 and the air mixed that comes from gas blower 8 by superheated vapour pipeline 13, as vaporized chemical and fluidizing medium, enter circulating fluidized bed from the sparger 5 of circulating fluidized bed main body 1 bottom, go into the stove coal dust in fluidized-bed with fast fluidizing high-temperature particle and the blending of gasification gas, the small particles coal dust upwards flows, high temperature 900-1000 ℃ pyrolysis, entering cyclonic separator 3 through gas-solid mixed pipe line 2 separates, middle particle returns the circulating fluidized bed lower body part through one-level material returning device 7, coal gas carries small-particle and comes out from cyclonic separator 3 is suitable for reading, enter superheated vapour interchanger 16 through coal gas of high temperature pipeline 19 and carry out heat exchange and separation, enter circulation separator 15 again, coal gas is from discharging for user's gas exit 18, the fine particle that superheated vapour interchanger 16 isolating small particles are separated through sedimentation pipeline 14 and circulation separator 15 enters air flow bed reactor 11 by secondary material returning device 12, the air of gas blower 8 enters air flow bed reactor 11 through air arm 10 and carries out oxidizing reaction, reaction back liquid slag enters circulating fluidized bed main body 1 interior bottom and mixes as heat of gasification with fluidized-bed bottom solid ash, low carbon containing lime-ash is arranged in airtight ash bucket via heat exchange type spiral ash ejector 6, regularly discharge slag, deliver to interim storage slag field through belt.
During operation, directly fall into furnace bottom downwards than coarse particles in circulating fluidized bed main body 1, in boiling shape furnace charge, violent mass transfer and heat transfer take place in gas, solid two-phase, and combustion reactions and steam reaction generation H take place
2, CO
2Deng, Wingdale has removed the sulphur in the coal gas as sweetening agent, and close phase section uniformity of temperature profile, temperature of reaction are 900-1100 ℃, significantly reduce coal tar, phenol and the light oil etc. that the back fast pyrogenation produces that are heated, and cracking mainly generates CH under the bed hot conditions
4Deng small molecules, all the other are gone into small-particle that stove fine powder and macrobead produce because of the cracking of being heated and are carried by reactant gases and leave close section mutually, freeboard of fluidized bed is formed at the top in circulating fluidized bed main body 1, cyclonic separator 3 separates the semicoke and the ash that obtain and is sent back to circulating fluidized bed main body 1 bottom through one-level material returning device 7 by water vapour, circulation separator 15 separates the fine powder that obtains and is brought into air flow bed reactor 11 through secondary material returning device 12 by water vapour and tangential introduction of air, spiral oblique current downflow generating gasification reaction, liquid slag and gas flow into circulating fluidized bed main body 1, low carbon containing lime-ash is arranged in airtight ash bucket via heat exchange type spiral ash ejector 6, regularly be discharged to the furnace bottom slag car, have bad luck again into the slag storehouse, deliver to interim storage slag field through short belt.
Claims (1)
1. a fine coal classification gasification is produced the method for coal gas, it is characterized in that: coal charge is sent in the center lumen of circulating fluidized bed main body by coal filling hole, superheated vapour from the superheated vapour interchanger, enter the air mixed of mixing tank and gas blower by the superheated vapour pipeline, enter circulating fluidized bed from the sparger of circulating fluidized bed bottom part body, go into the stove coal dust in fluidized-bed with fast fluidizing high-temperature particle and the blending of gasification gas, the small particles coal dust upwards flows, high temperature 900-1000 ℃ pyrolysis, entering cyclonic separator through the gas-solid mixed pipe line separates, middle particle returns the circulating fluidized bed lower body part through the one-level material returning device, coal gas carries small-particle and comes out from cyclonic separator is suitable for reading, enter the superheated vapour interchanger through the coal gas of high temperature pipeline and carry out heat exchange and separation, enter the circulation separator again, coal gas is from discharging for user's gas exit, the fine particle that the isolating small particles of superheated vapour interchanger is separated through sedimentation pipeline and circulation separator enters the air flow bed reactor by the secondary material returning device, the air of gas blower enters the air flow bed reactor for oxidation reactions through the air arm, the fine particle of separating enters the air flow bed reactor through the secondary material returning device, reaction back liquid slag enters the interior bottom of circulating fluidized bed main body mixes as heat of gasification with the solid ash, and low carbon containing lime-ash is arranged in airtight ash bucket via heat exchange type spiral ash ejector.
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| CN2011101857687A CN102277200A (en) | 2011-07-05 | 2011-07-05 | Method for preparing coal gas by virtue of pulverized coal grading gasification |
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| CN2011101857687A CN102277200A (en) | 2011-07-05 | 2011-07-05 | Method for preparing coal gas by virtue of pulverized coal grading gasification |
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Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102634372A (en) * | 2012-04-06 | 2012-08-15 | 中国科学院过程工程研究所 | Gasification method and device for preparing low-tar industrial coal gas by two-section furnace of fixed bed |
| CN102965139A (en) * | 2012-11-16 | 2013-03-13 | 中国石油大学(华东) | Heavy oil pyrolysis and gasification device coupling combined type lifting pipe and downstream reactor |
| CN102977928A (en) * | 2012-10-11 | 2013-03-20 | 田原宇 | Pulverized coal combined circulating fluidized bed hierarchical pyrolytic gasifier |
| CN103102990A (en) * | 2012-10-11 | 2013-05-15 | 田原宇 | Biomass abnormal circulating fluidized bed gasifier |
| CN103148513A (en) * | 2013-03-07 | 2013-06-12 | 华北电力大学（保定） | Biomass pyrolysis double fluidized bed ignition system and working method thereof |
| CN104109560A (en) * | 2013-09-30 | 2014-10-22 | 六盘水钟山区民富砖厂 | Method for preparing industrial fuel gas through pyrolysis treatment of garbage |
| CN104704088A (en) * | 2012-07-17 | 2015-06-10 | 派若尼耳有限公司 | Apparatus and methods for gasification |
| CN104736680A (en) * | 2012-06-29 | 2015-06-24 | 乔恩·雅各布森 | Method and apparatus for producing fuel gas from waste |
| CN105779008A (en) * | 2016-04-15 | 2016-07-20 | 安徽科达洁能股份有限公司 | Coal dust processing method and system |
| CN105838451A (en) * | 2016-04-26 | 2016-08-10 | 华陆工程科技有限责任公司 | Method for gasifying pulverized coal step by step in double beds connected in series |
| CN107880938A (en) * | 2016-09-30 | 2018-04-06 | 中国科学院工程热物理研究所 | Pre-heated classification gasification method and device |
| 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 |
| CN110791326A (en) * | 2019-11-21 | 2020-02-14 | 中国科学院工程热物理研究所 | Circulating fluidized bed gasification device with gasification auxiliary bed and gasification method |
| CN113462434A (en) * | 2021-07-06 | 2021-10-01 | 中国科学院工程热物理研究所 | Gasification method and system with fly ash regasification function |
| CN115029162A (en) * | 2022-08-10 | 2022-09-09 | 北京中瀚能源有限公司 | Gasification device and staged gasification method |
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| CN101440310A (en) * | 2007-11-23 | 2009-05-27 | 山东科技大学 | Process for fluidized bed classification gasification of dust coal |
| CN201574143U (en) * | 2009-11-20 | 2010-09-08 | 田原宇 | Grading gasification furnace of powdered coal circulating fluidized bed |
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| CN201574143U (en) * | 2009-11-20 | 2010-09-08 | 田原宇 | Grading gasification furnace of powdered coal circulating fluidized bed |
Cited By (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102634372B (en) * | 2012-04-06 | 2014-09-24 | 中国科学院过程工程研究所 | A fixed-bed two-stage furnace gasification method and device for preparing low-tar industrial gas |
| CN102634372A (en) * | 2012-04-06 | 2012-08-15 | 中国科学院过程工程研究所 | Gasification method and device for preparing low-tar industrial coal gas by two-section furnace of fixed bed |
| CN104736680A (en) * | 2012-06-29 | 2015-06-24 | 乔恩·雅各布森 | Method and apparatus for producing fuel gas from waste |
| CN104704088A (en) * | 2012-07-17 | 2015-06-10 | 派若尼耳有限公司 | Apparatus and methods for gasification |
| CN102977928A (en) * | 2012-10-11 | 2013-03-20 | 田原宇 | Pulverized coal combined circulating fluidized bed hierarchical pyrolytic gasifier |
| CN103102990A (en) * | 2012-10-11 | 2013-05-15 | 田原宇 | Biomass abnormal circulating fluidized bed gasifier |
| CN103102990B (en) * | 2012-10-11 | 2015-01-28 | 田原宇 | Biomass abnormal circulating fluidized bed gasifier |
| CN102965139A (en) * | 2012-11-16 | 2013-03-13 | 中国石油大学(华东) | Heavy oil pyrolysis and gasification device coupling combined type lifting pipe and downstream reactor |
| CN103148513A (en) * | 2013-03-07 | 2013-06-12 | 华北电力大学（保定） | Biomass pyrolysis double fluidized bed ignition system and working method thereof |
| CN104109560B (en) * | 2013-09-30 | 2017-02-01 | 六盘水钟山区民富砖厂 | Method for preparing industrial fuel gas through pyrolysis treatment of garbage |
| CN104109560A (en) * | 2013-09-30 | 2014-10-22 | 六盘水钟山区民富砖厂 | Method for preparing industrial fuel gas through pyrolysis treatment of garbage |
| CN105779008A (en) * | 2016-04-15 | 2016-07-20 | 安徽科达洁能股份有限公司 | Coal dust processing method and system |
| CN105838451A (en) * | 2016-04-26 | 2016-08-10 | 华陆工程科技有限责任公司 | Method for gasifying pulverized coal step by step in double beds connected in series |
| CN107880938A (en) * | 2016-09-30 | 2018-04-06 | 中国科学院工程热物理研究所 | Pre-heated classification gasification method and device |
| 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 |
| CN110791326A (en) * | 2019-11-21 | 2020-02-14 | 中国科学院工程热物理研究所 | Circulating fluidized bed gasification device with gasification auxiliary bed and gasification method |
| CN113462434A (en) * | 2021-07-06 | 2021-10-01 | 中国科学院工程热物理研究所 | Gasification method and system with fly ash regasification function |
| CN113462434B (en) * | 2021-07-06 | 2022-08-02 | 中国科学院工程热物理研究所 | A gasification method and system with fly ash regasification |
| CN115029162A (en) * | 2022-08-10 | 2022-09-09 | 北京中瀚能源有限公司 | Gasification device and staged gasification method |
| CN115029162B (en) * | 2022-08-10 | 2022-11-15 | 北京中瀚能源有限公司 | Gasification device and staged gasification method |
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Application publication date: 20111214 |