CN106590757A - Device and method for segmented-oxygen-blowing catalytic coal gasification - Google Patents
Device and method for segmented-oxygen-blowing catalytic coal gasification Download PDFInfo
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- 239000003245 coal Substances 0.000 title claims abstract description 104
- 238000002309 gasification Methods 0.000 title claims abstract description 62
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims description 24
- 238000007664 blowing Methods 0.000 title abstract 2
- 238000006243 chemical reaction Methods 0.000 claims abstract description 42
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 38
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 38
- 239000001301 oxygen Substances 0.000 claims abstract description 38
- 238000009826 distribution Methods 0.000 claims abstract description 25
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 15
- 239000002817 coal dust Substances 0.000 claims description 26
- 239000003054 catalyst Substances 0.000 claims description 25
- 239000000839 emulsion Substances 0.000 claims description 22
- 239000007789 gas Substances 0.000 claims description 15
- 230000011218 segmentation Effects 0.000 claims description 13
- 235000013312 flour Nutrition 0.000 claims description 9
- 230000008676 import Effects 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 7
- 210000003437 trachea Anatomy 0.000 claims description 6
- 230000015572 biosynthetic process Effects 0.000 claims description 4
- 230000001351 cycling effect Effects 0.000 claims description 4
- 238000003786 synthesis reaction Methods 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 3
- 239000002994 raw material Substances 0.000 claims description 3
- 238000006555 catalytic reaction Methods 0.000 claims description 2
- 230000003213 activating effect Effects 0.000 claims 1
- 230000004913 activation Effects 0.000 claims 1
- 238000007598 dipping method Methods 0.000 claims 1
- 230000003628 erosive effect Effects 0.000 claims 1
- 239000012530 fluid Substances 0.000 claims 1
- 238000000227 grinding Methods 0.000 claims 1
- 239000000203 mixture Substances 0.000 claims 1
- 238000012216 screening Methods 0.000 claims 1
- 238000003756 stirring Methods 0.000 claims 1
- 239000000843 powder Substances 0.000 abstract description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 9
- 229910052799 carbon Inorganic materials 0.000 abstract description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 238000005516 engineering process Methods 0.000 description 26
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 12
- 239000002956 ash Substances 0.000 description 10
- 238000000926 separation method Methods 0.000 description 8
- 230000018109 developmental process Effects 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 239000000428 dust Substances 0.000 description 4
- 239000003610 charcoal Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000011020 pilot scale process Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000004308 accommodation Effects 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 229910000272 alkali metal oxide Inorganic materials 0.000 description 1
- -1 alkali metal salt Chemical class 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
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- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The invention relates to a device for segmented-oxygen-blowing catalytic coal gasification. The device is mainly used for solving the problems that the temperature and concentration in a reactor are non-uniform in distribution and the efficiency of carbon conversion is relatively low. By a technical scheme that the device disclosed by the invention mainly comprises a gasifying agent inlet (1), an oxygen-enriched air inlet (7), a reactor dense-phase zone (13), a reactor dilute-phase zone (15), a primary cyclone separator (18) and a secondary cyclone separator (20), wherein the lower end of the fluidized-bed reactor dense-phase zone (13) is connected with an ash hopper (11), a lower part opening of the reactor dense-phase zone (13) is connected with a powder coal charging opening (3) and a primary powder coal circulating charging pipe (12), the primary cyclone separator (18) is connected with a reactor outlet (8), the secondary cyclone separator (20) is connected with the primary cyclone separator (18), and unreacted powder coal enters the reactor dilute-phase zone (15) through a secondary powder coal circulating charging opening (14), the technical problems are better solved, so that the device can be applied to the production of catalytic coal gasification industry.
Description
Technical field
The present invention relates to a kind of device and method with segmentation oxygen blast catalytic coal gasifaction.
Background technology
Coal, oil, natural gas are three big primary energy of the world, and wherein coal accounts for 79% in world's energy reserve, oil
12% is accounted for natural gas.Coal is to produce one of main fuel resource of power, heat, coal tar processing and by-product pitch.With stone
Oily resource it is increasingly in short supply, effectively utilizes coal resources become China's energy sustainable development one is tactful.But it is big at present
Amount coal is directly burnt, not only waste of resource but also pollution environment.At present, considerable part acid rain, flying dust, SOx and
The greenhouse gases of NOx.Therefore, the coal conversion technology for the purpose of reducing pollution receives greatly attention.Numerous
In coal utilization technology, coal gasification is the basic technology of Coal Energy Source conversion, and most important technique mistake in Development of Coal Chemical Industry
Journey.
At present, external industrialized Coal Gasification Technology can be divided three classes, i.e. the fixed bed gasification with Lurgi technologies as representative
Technology, the fluidized gasification technology with HTW technologies as representative, and with Texaco, Shell, multi-products production gasification skill
Art is the entrained flow bed gasification technology of representative.Airflow bed gasification furnace gasification temperature is high with pressure, load is big, coal wide accommodation,
It is the main flow of current Coal Gasification Technology development.External industrialized coal gasification entrained flow bed gasification technology mainly has
The GE Texaco gasification technologies of raw material, E～Gas gasification technologies, the Shell gasification technologies with dried coal powder as raw material, Prenflo
Gasification technology, GSP gasification technologies etc..The air-flow bed coal-gasification stove that external industrialization or document report have completed pilot scale is main
There are K～T gasification technologies, GSP gasification technologies etc..External industrialization or document report have completed the air flow bed coal gas of pilot scale
Changing stove mainly has K～T, Shell, Prenflo, GSP, Texaco, E～Gas, Eagle etc..Domestic air-flow bed coal-gasification skill
Art mainly has multi-products production gasification technology and two sections of dry coal powder gasification technologies.
China be one with the country that coal is main energy resource structure, will not change in the future for a long period of time.Realize coal
The efficient clean utilization of charcoal is countries in the world, and especially China realizes the key of energy sustainable development.When the energy that the whole world faces
Source and environmental problem, the development for New Coal Chemical provide unprecedented opportunities, at present, the coal gas chemical industry of comparative maturity
The gasification temperature of skill is general more than 1000 DEG C, this is because, Neng Gouman very fast in this temperature most of the above coal gasification speed
The requirement of sufficient practical application.These gasification technologies have the drawback that the high purification difficulty to generating gas of reaction temperature, energy consumption
It is big and high to equipment requirements, to generate the intensity of cooling of gas big etc., has thus directly promoted the research of catalytic coal gasifaction.
USP4,057,402 proposes a kind of fluidized gasification process, and coal is adopted in the laggard fluidized bed reactor of pretreatment
Lime-ash is excluded with ash agglomerating method, flying dust elder generation Jing stoves internal cyclone separators are separated, then Jing stove external cyclones separator is separated, and circulation contains
Carbon flying dust returns gasification installation, described gasification, stove internal cyclone separation under the condition of high temperature to be first passed through from molten poly- separating pipe
Device, so higher to its material requirement, flying dust is circulated by melting the separator for gathering ash, and operational control is difficult.
US4,077,778 proposes using multistage fluidized bed coal catalytic gasification technique, eliminates the deficiency of former catalysis gasification technique, makes
More efficient the carrying out of gasification, makes full use of charging carbon resource, improves efficiency of carbon con version.Main fluidized-bed operating gas velocity is higher, by portion
Divide carbon granule to carry secretly to secondary streams bed, gasification reaction is carried out under compared with low gas velocity, increase the time of staying of solid particle, most
Limits improve efficiency of carbon con version.Multistage fluidized bed coal catalytic gasification technique adopts multiple fluidized-bed reactors, and equipment investment is huge,
Operation is more complicated.
GPE companies of the U.S. are made further research on the basis of EXXON Technologies, and US20070000177AI is public
The technique for having opened coal one-step method methane, catalyst are alkali metal oxide or alkali metal salt, and gasifying agent is vapor, its master
Technical characteristic is wanted in addition to adding efficient methanation catalyst, calcium oxide is also added into in the middle of the coal dust of reaction, is absorbed
The carbon dioxide that course of reaction is produced, further improves methane content, and the determination of above-mentioned technique is due to adding methane to generate
Catalyst, but high temperature does not utilize the generation of methane, and, at 700 DEG C or so, response speed is slow for reaction temperature general control, needs
Being additionally provided heat maintains reaction temperature, these technologies to be also still in development.
In sum, main using traditional aeration operation in above-mentioned document, charcoal percent conversion is not high, unreacted coal dust amount compared with
Greatly, for subsequent technique purification, separation etc. bring huge difficulty, are susceptible to pipeline blockage phenomenon, cause the equipment can not
It is normal to run, and the present invention targetedly solves these problems.
The content of the invention
Present invention mainly solves one of technical problem be that temperature in pre-existing reactors, concentration distribution be uneven, efficiency of carbon con version is low
Problem, there is provided a kind of reaction unit of new catalytic coal gasifaction.In the combination unit fluidized-bed reactor have emulsion zone and
Freeboard temperature is evenly distributed, and charcoal percent conversion is high, the characteristics of after separation, ash content is high, simultaneously because the spy of this reactor
Different property so that the activity of its catalyst is higher, and coal ash can effectively discharge reactor, it is ensured that reaction it is efficient with it is stable.
The two of the technical problem to be solved be to provide it is a kind of with solve the corresponding reaction method of one of technical problem.
To solve one of above-mentioned technical problem, the technical solution used in the present invention is as follows：A kind of segmentation oxygen blast catalytic coal gasifaction is anti-
The device answered, mainly includes：Catalytic gasification ash separative element, catalytic coal gasifaction unit and unreacted coal dust cycling element structure
Into described catalytic gasification ash separative element is by gasifying agent air inlet pipe 26, circular cone distribution grid 2, coal dust charging aperture 3, center
Jet pipe 23, annular release pipe 24, ash bucket 11, slag-drip opening 9 are constituted, and circular cone distribution grid 2 is located at gasifying agent air inlet pipe 26
, in inverted cone, there are equally distributed gas outlet 27,2 lower end of circular cone distribution grid and annular point in top on circular cone distribution grid 2
From pipe 24 upper end connect, central jet pipe 23 be located at annular release pipe 24 centre, the lower end of annular release pipe 24 with
Ash bucket 11 is connected, and has annular release pipe air inlet 10 and slag-drip opening 9 on ash bucket 11；Described catalytic coal gasifaction unit has circle
Shape body of heater 4, reactor emulsion zone 13, reactor dilute-phase zone 15 are connected by reducing pipe 28, reactor emulsion zone 13
There are fine coal charging aperture 3 and one-level fine coal recycle feed pipe 12, reactor dilute-phase zone 15 has oxygen-enriched air import 7, second patent flour
Coal recycle feed mouth 14 and gasifier gas outlet 8；Described unreacted coal dust cycling element is by primary cyclone
18 and secondary cyclone 20 constitute, 18 bottom of primary cyclone is connected with one-level fine coal circulating solid tube 19, one
Level fine coal recycle feed pipe 12 and one-level returning charge trachea 16, it is vertical that 20 bottom of secondary cyclone is connected with the circulation of second patent flour coal
Pipe 21, second patent flour coal recycle feed pipe 14 and two grades of returning charge tracheas 17.
In above-mentioned technical proposal, the percent opening of the circular cone distribution grid 2 is 1%～2%, and aperture is 1～4mm, element of cone
Angle with central shaft is 30～45 °.The element of cone of reducing pipe 28 and the angle of centrage are 15～30 °.Reactor master
External body is connected to primary cyclone 18 and secondary cyclone 20, the coal dust circulation pipe of primary cyclone 18
12 are connected with reactor emulsion zone 13, at 30～60cm above circular cone distribution grid 2, in reactor emulsion zone 13
25～45 ° of heart wire clamp angle.The coal dust circulation pipe 14 of secondary cyclone 20 is connected with reactor dilute-phase zone 15, tapered
25～45 ° of centerlines above pipe 28 at 10～30cm, with reactor dilute-phase zone 15.Oxygen-enriched air import 7 is gradually
Above the draw 28 at 10～30cm, the centerlines with reactor dilute-phase zone 15 are 45～60 °.
For solve the above problems two, the technical solution used in the present invention is as follows：A kind of segmentation oxygen blast catalytic coal gasification
Method, using above-mentioned reaction unit, comprises the steps：
A 26 Jing circular cones distribution grid 2 of () gasifying agent autopneumatolysis agent air inlet pipe enters reactor emulsion zone 13, with supported catalyst
Coal dust mixing after reacted, produce synthesis gas, unreacted obtains coal dust and enters back into reactor dilute-phase zone 15, and from oxygen-enriched
The oxygen of air intlet 7 carries out part burning and regasifies reaction；
B () reacted product is carried treats unreacted coal dust and catalyst through primary cyclone 18 and two grades of whirlwind
Separator 20, the unreacted coal dust and catalyst after separation have respectively entered reactor emulsion zone 13 and reactor dilute-phase zone
Continue reaction in 15；
In above-mentioned technical proposal, the oxygen coal ratio is 0.3～1Nm3/ kg, steam coal weight ratio are 1～2.5, and granularity is
20～200 μm, the weight ratio of catalyst and coal is (0.05～0.20):1, oxygen enrichment percentage is 5～10%, and reactor emulsion zone 13 is warm
Degree maintains 750～850 DEG C, and 15 temperature of reactor dilute-phase zone maintains 650～800 DEG C, and 23 temperature of central jet pipe is maintained
Between 1300～1500 DEG C, reaction pressure is calculated as 0.1～3.5MPa with gauge pressure.
The device and method of segmentation oxygen blast catalytic coal gasification of the present invention.
Due in the course of reaction of catalytic coal gasifaction, it is desirable to which gas-solid carries out quick mixing contact, gasification temperature is stable.And ability
Well known to domain, general fluidized-bed reactor used in prior art, its feature is that reactor upper temp is too low, it is impossible to
Gasification reaction is carried out, is increased separation and is met and reaction time, it is totally unfavorable to reacting.Therefore using the segmentation reaction of the present invention
Device, which is similar to upper and lower reaction compartment temperature constant, gasification temperature is maintained convenient section, will so effectively improve anti-
Efficiency is answered, later separation burden is reduced, and then is improved gasification efficiency.
Using technical scheme：26 Jing circular cones distribution grid 2 of the gasifying agent autopneumatolysis agent air inlet pipe enters reactor
Emulsion zone 13, is reacted after being mixed with the coal dust of supported catalyst, produces synthesis gas, and unreacted obtains coal dust and enters back into reaction
Device dilute-phase zone 15, carries out part burning with the oxygen from oxygen-enriched air import 7 and regasifies reaction, and reacted product is carried
Treat unreacted coal dust and catalyst through primary cyclone 18 and secondary cyclone 20, the unreacted after separation
Coal dust and catalyst have respectively entered in reactor emulsion zone 13 and reactor dilute-phase zone 15 and continue reaction, it is ensured that fluidisation
Get along well on bed the uniform of temperature of lower, separated by two stage cyclone, it is to avoid the generation that catalyst is wasted, greatly improve carbon
Conversion ratio, achieve preferable technique effect.Methods described, than the efficiency of carbon con version in existing Winkler Coal Gasification Technologies
Improve 5～14%.
Description of the drawings
Schematic flow sheets of the Fig. 1 for the method for the invention：
In Fig. 1,1 is gasification agent inlet；2 is circular cone distribution grid；3 is coal dust charging aperture；4 are circular body of heater；5 is resistance to
Fiery material；6 is body of heater shell；7 is oxygen-enriched air import；8 export for gasifier gas；9 is slag-drip opening；10 are annular
Separating pipe air inlet；11 is ash bucket；12 is one-level fine coal recycle feed pipe；13 is reactor emulsion zone；14 is second patent flour
Coal recycle feed mouth；15 is reactor dilute-phase zone；16 is one-level returning charge trachea；17 is two grades of returning charge tracheas；18 is one-level
Cyclone separator；19 is one-level fine coal circulating solid tube；20 is secondary cyclone；21 is second patent flour coal circulating solid tube；
22 export for secondary cyclone；Jet pipe centered on 23；24 is annular release pipe；25 enter for oxygen-enriched annular release pipe
Mouthful；26 is gasifying agent air inlet pipe；27 is gas outlet.
26 Jing circular cones distribution grid 2 of gasifying agent autopneumatolysis agent air inlet pipe enters reactor emulsion zone 13, the coal with supported catalyst
Reacted after powder mixing, produced synthesis gas, unreacted obtained coal dust and enter back into reactor dilute-phase zone 15, and from oxygen-enriched air
The oxygen of import 7 carries out part burning and regasifies reaction, and reacted product is carried treats that unreacted coal dust and catalyst are passed through
Primary cyclone 18 and secondary cyclone 20, the unreacted coal dust and catalyst after separation have respectively entered instead
Continue reaction in answering device emulsion zone 13 and reactor dilute-phase zone 15.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Specific embodiment
【Embodiment 1】
In a kind of device of the segmentation oxygen blast catalytic coal gasifaction shown in Fig. 1, the mean temperature of fluidized-bed reactor is 750 DEG C,
The percent opening of circular cone distribution grid is 2%, and aperture is 4mm, and element of cone is 45 ° with the angle of central shaft, the circle of reducing pipe
The angle of cone nut line and centrage is 30 °, one cyclonic coal recycle feed pipe 30cm above the circular cone distribution grid, with reaction
The center angle of device emulsion zone is 25 °, two grades of whirlwind coal recycle feed pipes 10cm above the reducing pipe, with top dense-phase flow
The center angle for changing bed catalytic gasification section is 25 °, and coal powder size is 200 μm, and the load capacity of catalyst is 0.05, reaction
Device Stress control is kept bed mean temperature to fluctuate within ± 30 DEG C, is respectively joined after part operation condition and gasification in 1MPa
Number result is as shown in table 1.
【Embodiment 2】
In a kind of device of the segmentation oxygen blast catalytic coal gasifaction shown in Fig. 1, the mean temperature of fluidized-bed reactor is 750 DEG C,
The percent opening of circular cone distribution grid is 1%, and aperture is 1mm, and element of cone is 45 ° with the angle of central shaft, the circle of reducing pipe
The angle of cone nut line and centrage is 30 °, one cyclonic coal recycle feed pipe 30cm above the circular cone distribution grid, with reaction
The center angle of device emulsion zone is 25 °, two grades of whirlwind coal recycle feed pipes 10cm above the reducing pipe, with top dense-phase flow
The center angle for changing bed catalytic gasification section is 25 °, and coal powder size is 200 μm, and the load capacity of catalyst is 0.05, reaction
Device Stress control is kept bed mean temperature to fluctuate within ± 30 DEG C, is respectively joined after part operation condition and gasification in 1MPa
Number result is as shown in table 1.
【Embodiment 3】
In a kind of device of the segmentation oxygen blast catalytic coal gasifaction shown in Fig. 1, the mean temperature of fluidized-bed reactor is 750 DEG C,
The percent opening of circular cone distribution grid is 2%, and aperture is 4mm, and element of cone is 45 ° with the angle of central shaft, the circle of reducing pipe
The angle of cone nut line and centrage is 30 °, one cyclonic coal recycle feed pipe 30cm above the circular cone distribution grid, with reaction
The center angle of device emulsion zone is 25 °, two grades of whirlwind coal recycle feed pipes 10cm above the reducing pipe, with top dense-phase flow
The center angle for changing bed catalytic gasification section is 25 °, and coal powder size is 200 μm, and the load capacity of catalyst is 0.05, reaction
Device Stress control keeps bed mean temperature to fluctuate within ± 30 DEG C in 3.5MPa, each after part operation condition and gasification
Parametric results are as shown in table 1.
【Embodiment 4】
In a kind of device of the segmentation oxygen blast catalytic coal gasifaction shown in Fig. 1, the mean temperature of fluidized-bed reactor is 750 DEG C,
The percent opening of circular cone distribution grid is 2%, and aperture is 4mm, and element of cone is 45 ° with the angle of central shaft, the circle of reducing pipe
The angle of cone nut line and centrage is 30 °, one cyclonic coal recycle feed pipe 30cm above the circular cone distribution grid, with reaction
The center angle of device emulsion zone is 45 °, two grades of whirlwind coal recycle feed pipes 10cm above the reducing pipe, with top dense-phase flow
The center angle for changing bed catalytic gasification section is 45 °, and coal powder size is 200 μm, and the load capacity of catalyst is 0.05, reaction
Device Stress control is kept bed mean temperature to fluctuate within ± 30 DEG C, is respectively joined after part operation condition and gasification in 1MPa
Number result is as shown in table 1.
【Comparative example 1】
Conventional atmospheric Winkler coal gasifications temperature more than 950 DEG C, without reducing pipe, without two grades of whirlwind, the addition without catalyst,
Coal powder size is 0.1～3mm, and after part operation condition and gasification, each parametric results are as shown in table 1.
【Comparative example 2】
Conventional high-tension Winkler Coal Gasification Technology gasification temperature more than 1000 DEG C, without reducing pipe, without two grades of whirlwind, nothing
The addition of catalyst, coal powder size are 0.1～3mm, and after part operation condition and gasification, each parametric results are as shown in table 1.
Table 1
Claims (10)
1. it is a kind of segmentation oxygen blast catalytic coal gasifaction device, it mainly by catalytic gasification ash separative element, catalytic coal gasifaction list
Unit and unreacted coal dust cycling element are constituted, and described catalytic gasification ash separative element is by gasifying agent air inlet pipe (26), circle
Cone distribution grid (2), coal dust charging aperture (3), central jet pipe (23), annular release pipe (24), ash bucket (11),
Slag-drip opening (9) is constituted, and positioned at gasifying agent air inlet pipe (26) top, in inverted cone, circular cone is distributed circular cone distribution grid (2)
There is equally distributed gas outlet (27) on plate (2), circular cone distribution grid (2) lower end is upper with annular release pipe (24)
End connection, central jet pipe (23) is positioned at the centre of annular release pipe (24), lower end and the ash of annular release pipe (24)
Bucket (11) is connected, and has annular release pipe air inlet (10) and slag-drip opening (9) on ash bucket (11)；Described coal catalysis
Gasification unit includes circular body of heater (4), reactor emulsion zone (13), reactor dilute-phase zone (15), by reducing pipe
(28) connect, wherein, reactor emulsion zone (13) has fine coal charging aperture (3) and one-level fine coal recycle feed pipe (12),
Reactor dilute-phase zone (15) has oxygen-enriched air import (7), and second patent flour coal recycle feed mouth (14) and gasifier gas go out
Mouth (8)；Described unreacted coal dust cycling element is by primary cyclone (18) and secondary cyclone (20)
Constitute, primary cyclone (18) bottom is connected with one-level fine coal circulating solid tube (19), one-level fine coal recycle feed pipe
(12) and one-level returning charge trachea (16), secondary cyclone (20) bottom is connected with second patent flour coal circulating solid tube (21),
Second patent flour coal recycle feed pipe (14) and two grades of returning charge tracheas (17).
2. the device of oxygen blast catalytic coal gasifaction is segmented according to claim 1, it is characterised in that circular cone distribution grid (2)
Percent opening is 1%～2%, and aperture is 1～4mm, and element of cone is 30～45 ° with the angle of central shaft.
3. the device of oxygen blast catalytic coal gasifaction is segmented according to claim 1, it is characterised in that the circle of reducing pipe (28)
Cone nut line is 15～30 ° with the angle of centrage.
4. the device of oxygen blast catalytic coal gasifaction is segmented according to claim 1, it is characterised in that connect outside reactor body
There are primary cyclone (18) and secondary cyclone (20), the one-level fine coal of primary cyclone (18) is followed
Ring feed pipe (12) is connected with reactor emulsion zone (13), at 30～60cm above circular cone distribution grid (2), and anti-
Answer 25～45 ° of the centerlines of device emulsion zone (13).
5. the device of oxygen blast catalytic coal gasifaction is segmented according to claim 1, it is characterised in that secondary cyclone (20)
Second patent flour coal recycle feed pipe (14) be connected with reactor dilute-phase zone (15), 10～30cm above the reducing pipe (28)
Place, 25～45 ° of the centerlines with reactor dilute-phase zone (15).
6. the device of oxygen blast catalytic coal gasifaction is segmented according to claim 1, it is characterised in that oxygen-enriched air import (7)
At 10～30cm above reducing pipe (28), the centerlines with reactor dilute-phase zone (15) are 45～60 °.
7. a kind of method of segmentation oxygen blast catalytic coal gasifaction, is urged using any one the segmentation oxygen blast coal in claim 1～6
The device of activating QI, reaction method is：, through grinding, dipping, stirring, mix homogeneously is mixed for coal dust and catalyst
Coal dust and catalyst are entered in fluidized-bed reactor as raw material, are contacted with gasifying agent, are calculated as with gauge pressure in reaction pressure
0.1～3.5MPa, makes furnace temperature maintain between 650～850 DEG C, anti-in coal dust surface erosion, perforate, reduction by catalyst
Activation energy is answered, the product of synthesis gas and ash is converted coal into.
8. the method for oxygen blast catalytic coal gasifaction is segmented according to claim 7, it is characterised in that after coal dust is broken, Jing is dried
And screening, granularity is 20～200 μm, and the weight ratio of catalyst and coal is (0.05～0.20):1, it is the broken of 1～2mm with granularity
Initial fluidized bed material of the coal as fluid bed.
9. the method for oxygen blast catalytic coal gasifaction is segmented according to claim 7, it is characterised in that oxygen coal ratio is
0.3～1Nm3/ kg, steam coal weight ratio are 1～2.5, and the oxygen enrichment percentage of oxygen-enriched air import (7) is 5～10%.
10. the method for oxygen blast catalytic coal gasifaction is segmented according to claim 7, it is characterised in that reactor emulsion zone (13)
Temperature maintains 750～850 DEG C, and reactor dilute-phase zone (15) temperature maintains 650～800 DEG C, central jet pipe (23)
Temperature is maintained between 1300～1500 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510666051.2A CN106590757A (en) | 2015-10-15 | 2015-10-15 | Device and method for segmented-oxygen-blowing catalytic coal gasification |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510666051.2A CN106590757A (en) | 2015-10-15 | 2015-10-15 | Device and method for segmented-oxygen-blowing catalytic coal gasification |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106590757A true CN106590757A (en) | 2017-04-26 |
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| CN109628153A (en) * | 2019-01-24 | 2019-04-16 | 江苏普格机械有限公司 | The method and fluidized-bed gasification furnace of coal gasification efficiency can be improved |
| CN109694752A (en) * | 2019-03-01 | 2019-04-30 | 江苏普格机械有限公司 | The back powder method of fluidized bed and fluidized-bed gasification furnace based on this method |
| CN110205164A (en) * | 2019-06-11 | 2019-09-06 | 中国科学院工程热物理研究所 | Circulating fluidized bed gasification device and ciculation fluidized bed gasification method |
| CN110791294A (en) * | 2019-10-28 | 2020-02-14 | 北京国电富通科技发展有限责任公司 | Dust collecting and discharging device in pyrolysis furnace |
| CN112238004A (en) * | 2019-07-16 | 2021-01-19 | 中国石油化工股份有限公司 | Cyclone separator and pulverized coal fluidization gasification separation device |
| CN114507549A (en) * | 2022-02-21 | 2022-05-17 | 新疆天业汇合新材料有限公司 | Method for controlling slag bonding of coal gasification and radiation waste boiler combined device |
| CN114686268A (en) * | 2020-12-27 | 2022-07-01 | 新疆宜化化工有限公司 | A process for using oxygen-enriched circulating fluidized bed to realize coal gasification of raw materials with different characteristics of coal to syngas |
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