CN105273764A - Coal gasification apparatus and coal gasification method - Google Patents
Coal gasification apparatus and coal gasification method Download PDFInfo
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- CN105273764A CN105273764A CN201410355461.0A CN201410355461A CN105273764A CN 105273764 A CN105273764 A CN 105273764A CN 201410355461 A CN201410355461 A CN 201410355461A CN 105273764 A CN105273764 A CN 105273764A
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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Abstract
The present invention relates to a coal gasification apparatus and a coal gasification method under a catalyst loading condition. A purpose of the present invention is to solve the problems of high equipment requirement and high energy consumption caused by high coal gasification temperature, low carbon conversion rate and other process parameters in the prior art. The technical scheme of the present invention comprises that coal and a gasification agent are subjected to a gasification reaction under the effect of a catalyst, the apparatus mainly comprises a fluidized bed reactor (12), a cyclone separator (13), a heat exchange device (14) and a purification device (15), the fluidized bed reactor (12) is radially provided with a material inlet I (27) and a material inlet II (28), the bottom portion is provided with a gas inlet (24), the fluidized bed reactor (12) is divided into a lower portion dense phase region (26) and an upper portion dilute phase region (29), and the cyclone separator (13) comprises a J-shaped tube material feeding section (34) and a J-shaped tube material discharge section (35). According to the present invention, with the intermittent residue discharge, the coal powder low temperature gasification in the reaction equipment is achieved, the production cost of the synthesis gas is reduced, the equipment on the equipment is reduced, the catalyst is recycled, and the carbon conversion rate is improved; and with the technical scheme, the problems in the prior art can be well solved, and the apparatus and the method can be used for coal gasification in the industrial production.
Description
Technical field
The present invention relates to a kind of loading catalyst Coal Under gasification installation and gasification process.
Background technology
China is the country of the oil-poor deficency of rich coal, and along with the minimizing day by day of oil and natural gas resource, the clean coal conversion technology efficiently of development has far-reaching significance.
Traditional Coal Gasification Technology, namely the vaporized chemical that coal at high temperature forms with oxygen or air and water vapour gasifies, generate synthetic gas (mainly hydrogen, carbon monoxide and carbonic acid gas), roughly can be divided into three major types: high pressure fixed bed gasification, entrained flow gasification and fluidized-bed gasification etc.The temperature that this Coal Gasification Technology has needed for gasification reaction is high, and energy consumption is large, to shortcomings such as equipment requirements are high.
Loading catalyst Coal Under gasification installation and gasification process are a kind of important way of the clean efficiency utilization of coal, adopt catalytic coal gasifaction technology, the vaporized chemical that coal forms with water vapour, air or oxygen at relatively low temperature carries out gasification reaction under the effect of catalyzer, generate synthetic gas, this technology is compared with other Coal Gasification Technology, there is gasification temperature low, synthetic gas content is high, to advantages such as equipment Requirement condition are low.
This technology can make the material be fluidized fully mix with catalyzer, is conducive to heat transfer, mass transfer and gasification reaction, is conducive to the utilization of pulverulent material, but the loss simultaneously also bringing carbon in ash in discharge and cyclonic separator is larger waits deficiency.
USP4,057,402 propose a kind of fluidized-bed gasification process, coal through pre-treatment laggard enter in fluidized-bed reactor, adopt ash agglomerating method to get rid of lime-ash, flying dust is first separated through stove internal cyclone separators, then is separated through stove external cyclone separator, circulation carbon containing flying dust returns gasification installation from molten poly-separator tube, described gasification, first stove internal cyclone separators under the condition of high temperature, so require higher to its material, flying dust is circulated by the separator of molten poly-ash, and operation controls difficulty.
US4,077,778 propose to adopt multistage fluidized bed coal catalytic gasification technique, eliminate the deficiency of former catalysis gasification technique, gasification are carried out more efficiently, makes full use of feed carbon resource, improve efficiency of carbon conversion.Main fluidized-bed operating gas velocity is higher, is carried secretly by part carbon granule to secondary fluidized-bed, under comparatively low gas velocity, carry out gasification reaction, increases the residence time of solid particulate, improves efficiency of carbon conversion to greatest extent.Multistage fluidized bed coal catalytic gasification technique adopts multiple fluidized-bed reactor, and facility investment is huge, operates more complicated.
GPE company of the U.S. makes further research on EXXON Technology basis, US20070000177AI discloses the technique of coal single stage method methane, catalyzer is alkalimetal oxide or an alkali metal salt, vaporized chemical is water vapour, its technical characteristics is except adding efficient methanation catalyst, also add in the middle of calcium oxide to the coal dust of reaction, the carbonic acid gas that absorption reaction process produces, further raising methane content, the determination of above-mentioned technique is the catalyzer owing to adding methane generation, but high temperature does not utilize the generation of methane, temperature of reaction general control is at about 700 DEG C, speed of response is slow, need additionally to provide heat to maintain temperature of reaction, these technology are also still in development.
Summary of the invention
One of technical problem to be solved by this invention is the problem high to gasification temperature existed in prior art, proposes a kind of new coal gasification apparatus.This device may be used for gasification and produces, and has the gentleness gasification realizing coal, fluidizer simplicity of design, and then advantage low for equipment requirements simultaneously.
Two of technical problem to be solved by this invention there is the low problem of efficiency of carbon conversion in prior art, adopts above-mentioned coal gasification apparatus, proposes a kind of new coal gasification method.The method may be used for gasification and produces, and have temperature low, efficiency of carbon conversion is high, consumes low advantage to process energy consumption simultaneously.
For one of solving the problems of the technologies described above, the technical solution adopted in the present invention is as follows: a kind of loading catalyst Coal Under gasification installation, major equipment comprises disintegrating apparatus 7, grinding plant 8, mix and blend equipment 9, drying plant 10, fluidized-bed reactor 12, cyclonic separator 13, heat exchanging apparatus 14, treating plant 15, wherein fluidized-bed reactor 10 top is freeboard of fluidized bed 29 and bottom is emulsion zone 26, bottom emulsion zone 26 has radial opening for feed I 27 and opening for feed II 28, and air-distributing device 25 and inlet mouth 24 are equipped with in bottom; Freeboard of fluidized bed, top 29 has pneumatic outlet 30 and is connected to cyclonic separator 13, cyclonic separator 13 Nei You separate chamber 31, complete gas solid separation, type pipe blanking section that bottom has " J " 34 and " J " type pipe discharging section 35, Cyclone outlet 33 is connected with heat exchanging apparatus 14; Gas after heat exchange is by collecting after gas purifying equipment 16.
In technique scheme, described loading catalyst Coal Under gasification installation, is characterized in that coal and catalyzer complete in grinding plant, and described grinding plant is ball mill or colloidal mill.The freeboard of fluidized bed, top 29 of described fluidized-bed reactor 12 and the diameter ratio of bottom emulsion zone 26 are (2.0 ~ 10.5): 1; The ratio of height is (3.0 ~ 12.0): 1.The radial opening for feed I 27 of described bottom emulsion zone and opening for feed II 28 are 45 DEG C for being axially arranged symmetrically with horizontal sextant angle." J " type pipe blanking section (34) bottom of described cyclonic separator has ash discharging hole (36), and " J " type pipe discharging section (34) distance bottom ash discharging hole (36) is 30 ~ 60cm.
In the present invention, loading catalyst Coal Under gasification installation is proposed, object is better mixed coal powder and catalyzer, the unreacted pulverized coal particle of high efficiente callback, effective reduction gasification temperature and raising charcoal percent conversion, use the fluidized-bed reactor of simplicity of design simultaneously, and then make this technique be applicable to the coal gasification method of low cost and extensive process China rich reserves.
For solve the problems of the technologies described above two, the present invention's technical scheme used is as follows: coal dust and catalyzer are through grinding, dipping, stir, mix, mixed coal dust and catalyzer enter in fluidized-bed reactor as raw material, contact with vaporized chemical, 0.1 ~ 3MPa is counted with gauge pressure in reaction pressure, the medial temperature of conversion zone is 650 ~ 800 DEG C, gas velocity is under the condition of 0.1 ~ 0.6m/s, catalyzer is in coal dust surface erosion, perforate, reduce reaction activity, coal is converted into synthetic gas, the product of ash, the synthetic gas that temperature is higher passes through heat exchange recovery part heat.
In technique scheme, described catalyzer can be basic oxide, metal-salt, and wherein basic oxide can be Fe
2o
3, CaO, MgO, K
2o and Na
2at least one in O etc.; Metal-salt can be KCl, K
2cO
3, K
2sO
4and Na
2cO
3deng at least one.It is 20 ~ 200 μm that described coal dust and catalyzer are milled to granularity, and the weight ratio of catalyzer and coal is (0.05 ~ 0.20): 1.Described emulsion zone flow velocity is 0.4 ~ 0.6m/s, and freeboard of fluidized bed flow velocity is 0.1 ~ 0.4m/s.
In method of the present invention, coal dust and catalyzer are milled to designated size 20 ~ 200 μm, fully mix in mix and blend equipment, granules of catalyst is effectively attached on pulverized coal particle, the contact area of effective expansion coal dust, pulverized coal particle is allowed to expand the surface-area of micropore further when the later stage gasifies, catalyzer and coal form complex compound, reduce chemical energy, thus change reacting dynamics condition raising reaction efficiency, by the coal dust of attached catalyst, air or oxygen and water vapour join the emulsion zone of reactor lower part, emulsion zone is in gentle gasification reaction state, flow velocity is 0.4 ~ 0.6m/s, along with reaction is carried out, catalyzer is attached on semicoke and enters freeboard of fluidized bed, top, this region has the temperature of reaction of better gas-solid contact area and Geng Gao, advantageously in the gasification of semicoke, the flow velocity of freeboard of fluidized bed, top is more conducive to reaction, flow velocity is 0.1 ~ 0.4m/s, temperature is 650 ~ 800 DEG C, the particle (containing unreacted carbon and catalyzer etc.) being entered into cyclonic separator by freeboard of fluidized bed, top returns to reactor lower part emulsion zone through " J " type pipe discharging section and participates in reaction, while raising carbon turnover ratio, also make catalyzer be able to recycle.In addition due to the inventive method, temperature of reactor is significantly reduced, and achieves the gentleness gasification of coal, decrease equipment requirements and the process to cooling gas, make operation more convenient, effectively raise the utilization of energy, reduce thermosteresis, reduce the energy consumption of technique.
Be described above process unit of the present invention and method, but those skilled in the art obviously content according to the present invention can carry out a series of change to the present invention.Although the present invention focuses on elaboration coal prepare synthetic gas, obvious method of the present invention also can be used for processing refinery coke or biomass, also can be used for preparing coal tar wet goods simultaneously.The various change make the present invention or amendment, these equivalent form of values fall within patent requirements institute limited range appended by the application equally.
Adopt method of the present invention, achieve the gentleness gasification of coal, reduce the requirement of equipment for gasification and the consumption reducing energy in coal gasification course.Fluidized-bed reactor freeboard of fluidized bed and fluidized-bed reactor emulsion zone diameter ratio are 10.5:1, and the ratio of height is 12.0:1, and the medial temperature of fluidized-bed reactor is 800 DEG C, coal mean particle size is 100um, and catalyzer mean particle size is 100um, with this understanding, after gasification in gas composition, CO
2, CO, H
2and CH
4account for 2.8%, 56.1%, 25.2% and 13.2% of gas composition, charcoal percent conversion reaches 95%.
Accompanying drawing explanation
Fig. 1 is a kind of loading catalyst Coal Under gasification installation structural representation.
In Fig. 1,1 is coal; 2 is catalyzer; 3 is carrier gas; 4 is air (oxygen); 5 is water vapour; 6 is carrier gas; 7 is disintegrating apparatus; 8 is grinding plant; 9 is mix and blend equipment; 10 is moisture eliminator; 11 is feeding system; 12 is fluidized-bed reactor; 13 is cyclonic separator; 14 is interchanger; 15 is cleaner; 16 is container for storing liquid; 17 is preheater; 18 is ash discharge cinder notch; 19 is coal gas; 20 is heat recuperation.
Fig. 2 is the apparatus structure detailed annotation figure of feeding system, fluidized-bed reactor and cyclonic separator.In Fig. 2, (a) is the detailed annotation figure of the feeding system 11 in Fig. 1, and (b) is the detailed annotation figure of the fluidized-bed reactor 12 in Fig. 1, and (c) is the detailed annotation figure of the cyclonic separator 13 in Fig. 1, and wherein 21 is coal bunker; 22 is screw feeder; 23 is the outlet of feeding machine lower end; 24 is inlet mouth; 25 is air-distributing device; 26 is reactor emulsion zone; 27 is " J " type pipe returning charge entrance; 28 is furnace charge entrance; 29 is reactor freeboard of fluidized bed; 30 is syngas outlet; 31 is cyclonic separator separate chamber; 32 is cyclone inlet; 33 is Cyclone outlet; 34 is " J " type pipe blanking section; 35 is " J " type pipe discharging section; 36 is ash discharging hole.
Feed coal 1 is broken through disintegrating apparatus 7, and disintegrating apparatus 7 is connected with grinding plant 8, grinds, and catalyzer 2 (basic oxide or basic metal) enters in grinding plant 8 and grinds; Grinding plant 8 is connected with mix and blend equipment 9, carry out flooding, stirring in mix and blend equipment 9, by the coal bunker 21 added to after the coal mixed and the drying of catalyzer drying device 10 in feeding system 11, coal bunker 21 is connected to screw feeder 22 below, coal and catalyzer are carried by screw feeder 22, through feeding machine lower end outlet 23, deliver in reactor emulsion zone 26 and react; The synthetic gas generated and ash are after cyclonic separator 13 is separated, type pipe blanking section 34 that ash enters into " J ", pass through " J " type pipe discharging section 35 again, " J " type pipe discharging section 35 is connected with emulsion zone returning charge entrance 28, and last ash is back to reactor emulsion zone 26 and again fully gasifies; The slag that circulating fluid bed reactor produces is discharged from reactor bottom 24, and the gas separated enters into heat exchanging apparatus 14, and heat exchanging apparatus 14 is connected with purifier apparatus 15.
Below by embodiment, the present invention is further elaborated, but be not limited to and originally execute example.
Embodiment
[embodiment 1]
At Fig. 1, in technological reaction flow path device shown in 2, fluidized-bed reactor freeboard of fluidized bed and fluidized-bed reactor emulsion zone diameter ratio are 4.0:1, the ratio of height is 3.0:1, coal is preliminary broken at disintegrating apparatus warp, in grinding plant, be ground to mean particle size is 100um, it is 100um that catalyzer is ground to mean particle size in grinding plant, the medial temperature of fluidized-bed reactor is 700 DEG C, fluidized-bed reactor top pressure counts 0.1MPa with gauge pressure, the radial opening for feed of fluidized-bed reactor controls inlet amount by feeding system, axial admission mouth is with the amount of volume pump metering water vapour, in fluidized-bed reactor emulsion zone, linear gas velocity is 0.4m/s, and fluidized-bed reactor freeboard of fluidized bed linear gas velocity is 0.1m/s.Catalyzer is Na
2cO
3, the amount of catalyzer and the weight ratio of coal are 0.05:1, keep the fluctuation of bed medial temperature within ± 30 DEG C, after gasification in gas composition, and CO
2, CO, H
2and CH
4account for 2%, 57%, 28% and 10% of gas composition, all the other are unreacted O
2with rare gas element etc., charcoal percent conversion reaches 85%.
[embodiment 2]
According to the condition described in embodiment 1, the mean particle size of coal is 100um, the mean particle size of catalyzer is 100um, fluidized-bed reactor freeboard of fluidized bed and fluidized-bed reactor emulsion zone diameter ratio are 6.5:1, the ratio of height is 7.0:1, the medial temperature of fluidized-bed reactor is 750 DEG C, and fluidized-bed reactor top pressure counts 2.5MPa with gauge pressure, and catalyzer is Fe
2o
3, the amount of catalyzer and the weight ratio of coal are 0.10:1, keep the fluctuation of bed medial temperature within ± 30 DEG C, after gasification in gas composition, and CO
2, CO, H
2and CH
4account for 3%, 55%, 25% and 12% of gas composition, all the other are unreacted O
2with rare gas element etc., charcoal percent conversion reaches 90%.
[embodiment 3]
According to the condition described in embodiment 1, the mean particle size of coal is 100um, the mean particle size of catalyzer is 100um, fluidized-bed reactor freeboard of fluidized bed and fluidized-bed reactor emulsion zone diameter ratio are 10.5:1, the ratio of height is 12.0:1, the medial temperature of fluidized-bed reactor is 800 DEG C, and fluidized-bed reactor top pressure counts 3.0MPa with gauge pressure, and catalyzer is K
2cO
3, the amount of catalyzer and the weight ratio of coal are 0.15:1, keep the fluctuation of bed medial temperature within ± 30 DEG C, keep fluidized-bed reactor trouble-free operation, after gasification in gas composition, and CO
2, CO, H
2and CH
4account for 2.8%, 56.1%, 25.2% and 13.2% of gas composition, all the other are unreacted O
2with rare gas element etc., charcoal percent conversion reaches 95%.
[comparative example 1]
Conventional atmospheric Winkler Coal Gasification Technology gasification temperature, more than 950 DEG C, gasifies in rear gas composition, CO
2, CO, H
2and CH
4account for 17%, 25%, 32% and 0.8% of gas composition, all the other are unreacted O
2with rare gas element etc., charcoal percent conversion is only 81%.
[comparative example 2]
Conventional high-tension Winkler Coal Gasification Technology gasification temperature, more than 1000 DEG C, gasifies in rear gas composition, CO
2, CO, H
2and CH
4account for 8.2%, 48.2%, 30.6% and 2.8% of gas composition, all the other are unreacted O
2with rare gas element etc., charcoal percent conversion is 91%.
Claims (10)
1. a loading catalyst Coal Under gasification installation, major equipment comprises disintegrating apparatus (7), grinding plant (8), mix and blend equipment (9), drying plant (10), fluidized-bed reactor (12), cyclonic separator (13), heat exchanging apparatus (14), treating plant (15), wherein in fluidized-bed reactor (10), top is freeboard of fluidized bed (29), bottom is emulsion zone (26), bottom emulsion zone (26) has radial opening for feed I (27), opening for feed II (28), air-distributing device (25) and inlet mouth (24) are equipped with in bottom, freeboard of fluidized bed, top (29) has pneumatic outlet (30) and is connected to cyclonic separator (13), cyclonic separator (13) Nei You separate chamber (31), complete gas solid separation, " J " type pipe blanking section (34) and " J " type pipe discharging section (35) is arranged at cyclonic separator (13) bottom, and Cyclone outlet (33) is connected with heat exchanging apparatus (14), gas after heat exchange is collected afterwards by gas purifying equipment (16).
2. loading catalyst Coal Under gasification installation according to claim 1, is characterized in that coal and catalyzer grind in grinding plant, and described grinding plant is ball mill or colloidal mill.
3. loading catalyst Coal Under gasification installation according to claim 1, is characterized in that the diameter ratio of fluidized-bed reactor (12) freeboard of fluidized bed, top (29) and bottom emulsion zone (26) is for (2.0 ~ 10.5): 1; The ratio of height is (3.0 ~ 12.0): 1.
4. loading catalyst Coal Under gasification installation according to claim 1, it is characterized in that air-distributing device (25) is equipped with in fluidized-bed reactor (12) bottom, its hole is triangle, hexagon or circle.
5. loading catalyst Coal Under gasification installation according to claim 1, it is characterized in that described bottom emulsion zone (26) radial direction has two opening for feeds at least, opening for feed I (27) and opening for feed II (28), and be 45 DEG C for being axially arranged symmetrically with horizontal sextant angle.
6. loading catalyst Coal Under gasification installation according to claim 1, it is characterized in that " J " type pipe blanking section (34) bottom of cyclonic separator has ash discharging hole (36), " J " type pipe discharging section (34) distance bottom ash discharging hole (36) is 30 ~ 60cm.
7. a loading catalyst Coal Under gasification process, adopt the device of claim 1 ~ 7, reaction method is: coal dust and catalyzer are through grinding, dipping, stir, mix, mixed coal dust and catalyzer enter in fluidized-bed reactor as raw material, contact with vaporized chemical, 0.1 ~ 3MPa is counted with gauge pressure in reaction pressure, the medial temperature of conversion zone is 650 ~ 800 DEG C, gas velocity is under the condition of 0.1 ~ 0.6m/s, catalyzer is in coal dust surface erosion, perforate, reduce reaction activity, coal is converted into synthetic gas, the product of ash, the synthetic gas that temperature is higher passes through heat exchange recovery part heat.
8. loading catalyst Coal Under gasification process according to claim 7, it is characterized in that catalyzer is basic oxide or metal-salt, wherein basic oxide are Fe
2o
3, CaO, MgO, K
2o and Na
2at least one in O; Metal-salt is KCl, K
2cO
3, K
2sO
4and Na
2cO
3in at least one.
9. loading catalyst Coal Under gasification process according to claim 7, it is characterized in that coal dust and catalyzer are milled to granularity is 20 ~ 200 μm, and the weight ratio of catalyzer and coal is (0.05 ~ 0.20): 1.
10. loading catalyst Coal Under gasification process according to claim 7, it is characterized in that emulsion zone flow velocity is 0.4 ~ 0.6m/s, freeboard of fluidized bed flow velocity is 0.1 ~ 0.4m/s.
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|---|---|---|---|
| CN201410355461.0A CN105273764B (en) | 2014-07-24 | 2014-07-24 | Coal gasification apparatus and gasification process |
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|---|---|---|---|
| CN201410355461.0A CN105273764B (en) | 2014-07-24 | 2014-07-24 | Coal gasification apparatus and gasification process |
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| CN105273764B CN105273764B (en) | 2018-06-08 |
Family
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108018088A (en) * | 2016-10-28 | 2018-05-11 | 中国石油化工股份有限公司 | A kind of method of catalytic coal gasifaction |
| CN108179032A (en) * | 2018-01-09 | 2018-06-19 | 新奥科技发展有限公司 | A kind of fluidized-bed gasification furnace, gasification system and method |
| CN108342222A (en) * | 2017-01-24 | 2018-07-31 | 杨秋良 | Application process of the vanadium based gas catalyst on coal-fired industry fluid bed or air flow bed |
| CN108410506A (en) * | 2018-04-13 | 2018-08-17 | 新奥科技发展有限公司 | A kind of anaerobic catalytic gasification stove, catalytic gasification system and coal methanation process |
| CN110373230A (en) * | 2019-07-29 | 2019-10-25 | 安徽工业大学 | A kind of method that fluidized gasification flying dust returns furnace gas |
| CN111057585A (en) * | 2018-10-17 | 2020-04-24 | 中国石油化工股份有限公司 | Method for fluidized coal gasification |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108018088A (en) * | 2016-10-28 | 2018-05-11 | 中国石油化工股份有限公司 | A kind of method of catalytic coal gasifaction |
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| CN108410506A (en) * | 2018-04-13 | 2018-08-17 | 新奥科技发展有限公司 | A kind of anaerobic catalytic gasification stove, catalytic gasification system and coal methanation process |
| CN108410506B (en) * | 2018-04-13 | 2020-04-21 | 新奥科技发展有限公司 | Anaerobic catalytic gasification furnace, catalytic gasification system and coal methanation method |
| CN111057585A (en) * | 2018-10-17 | 2020-04-24 | 中国石油化工股份有限公司 | Method for fluidized coal gasification |
| CN110373230A (en) * | 2019-07-29 | 2019-10-25 | 安徽工业大学 | A kind of method that fluidized gasification flying dust returns furnace gas |
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| CN105273764B (en) | 2018-06-08 |
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