CN105441137A - Gasification reactor - Google Patents
Gasification reactor Download PDFInfo
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- CN105441137A CN105441137A CN201511001343.0A CN201511001343A CN105441137A CN 105441137 A CN105441137 A CN 105441137A CN 201511001343 A CN201511001343 A CN 201511001343A CN 105441137 A CN105441137 A CN 105441137A
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- Prior art keywords
- catalyzer
- gasifying reactor
- catalyst
- jet pipe
- arm
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- 238000002309 gasification Methods 0.000 title claims abstract description 71
- 238000009825 accumulation Methods 0.000 claims abstract description 51
- 239000003054 catalyst Substances 0.000 claims abstract description 37
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 29
- 239000012159 carrier gas Substances 0.000 claims abstract description 16
- 239000010410 layer Substances 0.000 claims description 21
- 239000011229 interlayer Substances 0.000 claims description 8
- 239000007789 gas Substances 0.000 description 32
- 239000003245 coal Substances 0.000 description 23
- 238000005516 engineering process Methods 0.000 description 16
- 238000006555 catalytic reaction Methods 0.000 description 13
- 238000000034 method Methods 0.000 description 12
- 239000007921 spray Substances 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 10
- 239000000463 material Substances 0.000 description 9
- 230000008569 process Effects 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- 239000002994 raw material Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 239000002956 ash Substances 0.000 description 4
- 239000002817 coal dust Substances 0.000 description 4
- 239000003034 coal gas Substances 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 239000002893 slag Substances 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 239000011449 brick Substances 0.000 description 3
- 239000003575 carbonaceous material Substances 0.000 description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 3
- 238000005507 spraying Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000002802 bituminous coal Substances 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000003250 coal slurry Substances 0.000 description 2
- 239000000567 combustion gas Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000010791 quenching Methods 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 230000003245 working effect Effects 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 235000010627 Phaseolus vulgaris Nutrition 0.000 description 1
- 244000046052 Phaseolus vulgaris Species 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/482—Gasifiers with stationary fluidised bed
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/723—Controlling or regulating the gasification process
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0983—Additives
- C10J2300/0986—Catalysts
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/12—Heating the gasifier
- C10J2300/1269—Heating the gasifier by radiating device, e.g. radiant tubes
-
- 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]
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention provides a gasification reactor which comprises a gasifying agent jet pipe, heat-accumulation radiant tubes and a catalyst addition assembly, wherein the gasifying agent jet pipe extends into the upper part in the gasification reactor through the top wall of the gasification reactor; the heat-accumulation radiant tubes are arranged into multiple layers along the gasification reactor, and each layer has a plurality of heat-accumulation radiant tubes which are parallel in the horizontal direction; the catalyst addition assembly comprises a catalyst hopper, a catalyst main pipe, a catalyst branch pipe, one or a plurality of catalyst jet parts and a carrier gas delivery part; the catalyst main pipe is arranged outside the gasification reactor and communicated with the catalyst hopper; the catalyst branch pipe penetrates through the side wall of the gasification reactor and extends to the inside of the gasification reactor; the catalyst branch pipe is communicated with the catalyst main pipe; the catalyst jet part or catalyst jet parts is/are arranged on the catalyst branch pipe, and positioned inside the gasification reactor; and the carrier gas delivery part is communicated with the catalyst main pipe. The gasification reactor can obviously enhance the gasification efficiency.
Description
Technical field
The present invention relates to the gasification process system designing a kind of carbonaceous material, especially a kind of gasification reaction apparatus.
Background technology
Large-scale Coal Gasification Technology is the core technology of Coal Clean Efficient Conversion, being the basis of development coal-based chemicals synthesis (ammonia, methyl alcohol, acetic acid, alkene etc.), liquid fuel synthesis (dme, gasoline, diesel oil etc.), the advanced process industrial such as IGCC power generation system, polygenerations systeme, hydrogen manufacturing, fuel cell, direct reduction iron making, is the common techniques of these industries, gordian technique and leading technology.At present, industrialized Coal Gasification Technology can be divided into 3 classes, namely with the Lurgi technology fixed bed gasification technology that is representative, with the HTW technology fluidized-bed gasification technology that is representative and the entrained flow bed gasification technology that is representative with Texaco, Shell, multi-products production gasification technology.
In Germany Lurgi-Spuelgas low temperature gasification technique, Lurgi stove is a kind of fixed bed pressured gasification stove.Strictly speaking, Lurgi pressurized-gasification furnace belongs to first-generation Coal Gasification Technology, but has constantly been improved since invention, still has extensive use so far in South Africa.Lurgi gasifying process has following characteristics: (1) uses the beans of granularity between 5 ~ 50mm; (2) may gasify from brown coal to anthracitic various coal, but the performance index such as thermostability, physical strength, binding agent of raw material be there are certain requirements; (3) working pressure is from 2 ~ 3MPa; (4) during gasification bituminous coal, CO:15% ~ 25% in raw gas; CO
2: 24% ~ 34%; H
2: 34% ~ 40%; CH
4: 9% ~ 13%; (5) furnace top gas temperature 250 ~ 350 DEG C; (6) single stove gas production rate 30000 ~ 50000Nm3/h; (7) cold gas efficiency can reach 80%.As can be seen from above process characteristic, the gas temperature of Lurgi is lower, in coal gas CH4 and tar content higher, raw gas purifying and tar processing unit are inevitable, and the environmental issue caused thus is more outstanding.From coal gas composition, Lurgi is best suited for the gas producing technology in direct-reduction, as long as just can directly for reduction shaft furnace after carrying out carbonization treatment to coal gas.But (1) furnace top gas temperature is low, in coal gas methane and tar content high, gas purification and sewage treatment process complexity, long flow path, equipment are many, slag carbon containing about 5%; (2) subsequent disposal operation need increase raw gas purifying and tar processing unit, and cost of investment increases; (3) lurgi stove belongs to fixed bed gasification technology, and its coal requires high, other process troubles of gas; (4) gasification furnace structure is complicated, is provided with broken the rotating machinerys such as glutinous and coal sparger, fire grate in stove, manufacture and maintenance cost; (5) the longlyest 5 ~ 6 months are only the work-ing life of the upper and lower valve of charging ash lock, and long-term dependence on import.
TEXACO coal slurry gasifier is the Coal Gasification Technology that Texaco company of the U.S. develops on heavy oil gasification basis, the s-generation entrained flow gasification technique that current business performance is maximum, technical characteristics is as follows: the coal water slurry that (1) charging adopts more than 75%-200 order coal dust to make, and in coal slurry, pulverized coal reburning is 65 ~ 70%.Texaco can be used for various coal gasification in theory, but experience shows optimum coal should to be ash fusion point be about 1300 DEG C, ash content lower than 20% coal; (2) vapor pressure is from 2.6 ~ 8.4MPa; (3) efficiency of carbon conversion is more than 95%, and cold gas efficiency can reach more than 70%; (4) (the CO+H in dry gas
2) effectively gas composition is more than 80%, CO accounts for 49%, H2 and accounts for 31%, CO
2account for 18% (Datong coal); (5) gasification temperature reaches 1300 ~ 1400 DEG C, and the raw gas temperature after water Quench is 200 ~ 260 DEG C.If adopt heat recovery type vapourizing furnace, after the temperature heat exchange of raw gas, be down to 400 DEG C from 1370 DEG C; (6) adopt single nozzle, hot wall stove apparatus-form, nozzle life on average at 1500h, the resistance to material life-span in 1 ~ 2 year, so must redundant system be provided with; (7) 1000Nm3 (CO+H is produced
2) the oxygen consumption of effective gas is at about 400Nm3, coal consumption is at about 640kg; (8) single stove design maximum day process coal amount can reach 2000t.Also there is more shortcoming in prior art: (1) coal water slurry charging, limits the scope of application of raw material, adds coal consumption and oxygen consumes; (2) adopt refractory brick hot wall stove, require higher to brick, changing brick affects working rate; (3) liquid slag proposes restriction to coal ash yield temperature; (4) nozzle life is relatively short.
Therefore, existing gasification technology is further improved.
Summary of the invention
The present invention is intended to solve one of technical problem in correlation technique at least to a certain extent.For this reason, one object of the present invention is to propose the high and gasifying reactor that energy consumption is low of a kind of gasification efficiency.
According to an aspect of the present invention, the present invention proposes a kind of gasifying reactor, the gasifying reactor according to the embodiment of the present invention comprises:
Gasification agent nozzle, described gasification agent nozzle stretches to the top in described gasifying reactor by the roof of described gasifying reactor, the outlet side of described gasification agent nozzle tapered and cone the end down;
Heat accumulation type radiant tube, it is inner that described heat accumulation type radiant tube is arranged in described gasifying reactor, and arrange along the short transverse multilayer of described gasifying reactor, and every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction;
Catalyzer adds assembly, and described catalyzer adds assembly and comprises:
Catalyst hooper;
Catalyzer is responsible for, and described catalyzer supervisor is arranged on outside described gasifying reactor vertically; Described catalyzer supervisor is connected with described catalyst hooper;
Catalyzer arm, described catalyzer arm through described gasifying reactor sidewall and extend to the inside of described gasifying reactor, described catalyzer arm is responsible for described catalyzer and is connected;
One or more catalyst ejector part, described catalyst ejector part is arranged on described catalyzer arm, and it is inner to be positioned at described gasifying reactor,
Part is sent in carrier gas, and described carrier gas is sent part and is responsible for described catalyzer and is connected, and described carrier gas is sent part and is configured to be suitable for catalyzer to be blown into described gasifying reactor.
This gasifying reactor adopts heat accumulation type radiant tube thus, and reaction process is simple, and inside reactor uniform temperature fields, can realize subregion temperature control, system thermal efficiency is high; Secondly, adopt catalyzer to add assembly and send into catalyzer in gasifying reactor, can catalysis carbonaceous material fuel gasification effectively.Therefore, the gasifying reactor of the above embodiment of the present invention is adopted to significantly improve gasification efficiency.
In addition, gasifying reactor according to the above embodiment of the present invention can also have following additional technical characteristic:
In some embodiments of the present invention, described catalyzer arm is multiple, and the length direction be responsible for along described catalyzer is arranged parallel to each other.
In some embodiments of the present invention, described catalyzer arm is responsible for perpendicular to described catalyzer.
In some embodiments of the present invention, described catalyzer arm extends to the whole layer width of described heat accumulation type radiant tube layer.
In some embodiments of the present invention, described catalyst ejector part comprises catalyzer jet pipe and is arranged on nozzle on described catalyzer jet pipe, and described nozzle is provided with variable valve, and optionally, described catalyzer jet pipe is U-shaped, S type or W type jet pipe.
In some embodiments of the present invention, described catalyst ejector part comprises catalyzer jet pipe, and the tube wall of described catalyzer jet pipe is provided with through hole, and optionally, described catalyzer jet pipe is U-shaped, S type or W type jet pipe.
In some embodiments of the present invention, described catalyzer arm is arranged on the interlayer of described heat accumulation type radiant tube.
In some embodiments of the present invention, described catalyst ejector part is arranged in the interlayer of described heat accumulation type radiant tube.
In some embodiments of the present invention, the end that part is connected to described catalyzer supervisor is sent in described carrier gas.
In some embodiments of the present invention, described carrier gas send part removably connect or be soldered to described catalyzer supervisor.
In some embodiments of the present invention, the outlet side of described gasification agent nozzle is tapered and taper base angle is identical with the roof angle of inclination of described reactor.The mixture homogeneity of vaporized chemical and raw material can be improved thus further.
Accompanying drawing explanation
Fig. 1 is the structural representation of gasifying reactor according to an embodiment of the invention.
Fig. 2 is the structural representation of the gasification agent nozzle according to an embodiment of the invention in gasifying reactor.
Fig. 3 is the structural representation of the catalyzer jet pipe according to an embodiment of the invention in gasifying reactor.
Embodiment
Be described below in detail embodiments of the invention, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has element that is identical or similar functions from start to finish.Be exemplary below by the embodiment be described with reference to the drawings, be intended to for explaining the present invention, and can not limitation of the present invention be interpreted as.
According to an aspect of the present invention, the present invention proposes a kind of gasifying reactor.Describe the gasifying reactor of the specific embodiment of the invention below with reference to Fig. 1 in detail, comprising: gasification agent nozzle 20, heat accumulation type radiant tube 30 and catalyzer add assembly 40.
According to a particular embodiment of the invention, reactor has opening for feed 11, slag-drip opening 12 and gasification gas outlet 13, opening for feed 11 is arranged on the top of described reactor, and described slag-drip opening 12 is arranged on the bottom of described reactor, and described gasification gas outlet 13 is arranged on the sidewall of described reactor.
According to embodiments of the invention, the height of described reactor is 5 ~ 20m, and the width of described reactor is 2 ~ 8m.Thus, being gasified totally to material can be realized.
According to a particular embodiment of the invention, gasification agent nozzle 20 stretches to the top in described reactor by the roof of described reactor, the outlet side of described gasification agent nozzle tapered and cone the end down.Effectively can spray into vaporized chemical in reactor by this gasification agent nozzle 20 thus, and then react with the coal dust generating gasification that the opening for feed 11 of reactor adds, output gasification gas.
According to concrete example of the present invention, as shown in Figure 2, the outlet side of described gasification agent nozzle is tapered and taper base angle is identical with the roof angle of inclination of described reactor, and the outlet side diameter D of described gasification agent nozzle is 1/40 ~ 1/20 of described reactor width.Reactor top wall angle of inclination refers to the angle of reactor top wall internal surface and horizontal plane.Reactor width refers to the width W for the reactor upright wall part shown in Fig. 1 divides.Thus by taper is arranged in the outlet side of gasification agent nozzle, and then improve the area spraying into vaporized chemical, effectively improve itself and the mixed uniformly efficiency of coal dust.In addition, contriver finds, specifically taper is arranged to taper base angle identical with the roof angle of inclination of described reactor, and outlet side diameter D is 1/40 ~ 1/20 of described reactor width, fully can mix with the coal dust that top adds gradually, and then significantly improve the spraying efficiency of vaporized chemical, the uniformity coefficient of spraying.
According to a particular embodiment of the invention, it is inner that heat accumulation type radiant tube 30 is arranged in described gasifying reactor, and spaced apart along height for reactor direction, and every layer of described heat accumulation type radiant tube 30 comprises multiple heat accumulation type radiant tube spaced apart in the horizontal direction.Adopt heat accumulation type radiant tube, heat smoke and the fuel and the air heat-exchange that enter combustion chamber, reduce funnel temperature, and heat transfer efficiency improves, and capacity usage ratio is high.
According to concrete example of the present invention, every layer of described heat accumulation type radiant tube comprises multiple parallel and equally distributed heat accumulation type radiant tube and each described heat accumulation type radiant tube is parallel with each heat accumulation type radiant tube in adjacent upper and lower two-layer heat accumulation type radiant tube.
According to embodiments of the invention, heat accumulation type radiant tube 30 is spaced apart along height for reactor direction in reactor, and every layer of heat accumulation type radiant tube comprises multiple heat accumulation type radiant tube spaced apart in the horizontal direction, according to a particular embodiment of the invention, every layer of heat accumulation type radiant tube comprises multiple parallel and equally distributed heat accumulation type radiant tube and each heat accumulation type radiant tube is parallel with each heat accumulation type radiant tube in adjacent upper and lower two-layer heat accumulation type radiant tube.According to concrete example of the present invention, heat accumulation type radiant tube is the circle of caliber 200 ~ 300mm or semicircle radiator tube.Thus, the gasification efficiency of material can be significantly improved, and then improve gasification gas productive rate.
According to embodiments of the invention, the horizontal throw between adjacent described heat accumulation type radiant tube center is 300 ~ 500mm, and the vertical range between mutually adjacent described heat accumulation type radiant tube center is 500 ~ 900mm.It should be explained that, horizontal throw between adjacent heat accumulation type radiant tube center can be understood as the distance on same layer between heat accumulation type radiant tube center, and the vertical range between adjacent heat accumulation type radiant tube center can be understood as adjacent upper and lower two interlayers adjacent heat accumulation type radiant tube center between distance.
According to embodiments of the invention, the number of plies of heat accumulation type radiant tube can be 5-15 layer.Contriver finds, this kind of structural arrangement can make uniform distribution of temperature field in gasification reaction district, thus can significantly improve the gasification efficiency of material, and then improves the yield of gasification gas.
According to embodiments of the invention, heat accumulation type radiant tube can be unidirectional regenerative gas radiator tube, and the heat namely produced by combustion gas by radiator tube body carries out heat supply in the mode of radiation.According to a particular embodiment of the invention, heat accumulation type radiant tube can be provided with gas control valve (not shown).Thus, by controlling to enter the air of radiator tube, gas quantity and proportioning thereof, radiator tube surface temperature is controlled, control the temperature required field of reaction, realize the accurate temperature controlling to gasification, thus the gasification efficiency of material can be significantly improved, and then improve the yield of gasification gas.Radiator tube combustion produce high-temperature flue gas, through with enter the low temperature control heat exchange of radiator tube, reduce funnel temperature, improve efficiency of combustion.
Concrete, the accurate temperature controlling of the realizations such as the flow of the combustion gas of heat accumulation type radiant tube to gasification can be passed into by adjustment, and heat accumulation type radiant tube adopts the combustion system of regularly commutation, the temperature field of single radiator tube is made to be more or less the same in 30 DEG C, and there is no partial insulation district, thus ensure the homogeneity in temperature field in reactor.
According to a particular embodiment of the invention, catalyzer adds assembly 40 and comprises: catalyst hooper 41; Catalyzer supervisor 42, catalyzer arm 43, one or more catalyst ejector part 44, part (not shown) is sent in carrier gas, and wherein, catalyzer supervisor 42 is arranged on outside gasifying reactor vertically; Catalyzer supervisor be connected with catalyst hooper; Described catalyzer arm is responsible for described catalyzer and is connected, described catalyzer arm through described gasifying reactor wall and extend to the inside of described gasifying reactor; Described catalyst ejector part is arranged on described catalyzer arm, and it is inner to be positioned at described gasifying reactor, and carrier gas is sent part and is responsible for described catalyzer and is connected.
According to concrete example of the present invention, catalyzer arm 43 is multiple, and arranged parallel to each other along the length direction of catalyzer supervisor.According to concrete example of the present invention, described catalyzer arm is responsible for perpendicular to described catalyzer.According to concrete example of the present invention, described catalyzer arm extends to the whole layer width of described heat accumulation type radiant tube layer.Multiple catalyzer arm can effectively ensure that catalyzer is uniformly distributed in reactor, and effectively ensures reaction raw materials Homogeneous phase mixing, thus ensures good catalyzed reaction effect.Meanwhile, catalyzer arm and radiator tube are arranged in parallel and can effectively prevent catalyzer from propping up blockage under being positioned at radiator tube.
According to concrete example of the present invention, the nozzle that described catalyst ejector part 44 comprises catalyzer jet pipe 441 and is arranged on described catalyzer jet pipe 441, nozzle is provided with variable valve.
According to concrete example of the present invention, as shown in Figure 3, catalyzer jet pipe 441 can be made up of multiple spaced apart in the horizontal direction and connected successively from beginning to end multiple muonic catalysis agent jet pipes 442, and the tube wall of each muonic catalysis agent jet pipe has multiple catalyzer spray orifice 443.Adopt the catalyzer coil pipe of special shape thus, the catalyzer come by catalyzer arm is carried by rare gas element and sprays in gasifying reactor in catalyzer jet pipe.Can catalyzer be evenly distributed in gasifying reactor, with gasified raw material Homogeneous phase mixing, and then catalytic gasification reaction, improve gasification efficiency.
According to concrete example of the present invention, catalyst ejector part 44 comprises catalyzer jet pipe 441, and the tube wall of catalyzer jet pipe is provided with through hole.
According to concrete example of the present invention, one end of catalyzer arm is removably connected to catalyzer supervisor and is above also communicated with it, one end of catalyzer jet pipe is communicated with the other end of catalyzer arm, the other end of catalyzer jet pipe is fixed on furnace wall, thus, catalyzer jet pipe is across gasifying reactor inside on the width of reactor.The bottom of catalyzer supervisor is communicated with gas reservoir.Rare gas element is blown into catalyzer supervisor by gas reservoir, thus catalyzer is blown into catalyzer jet pipe.Rare gas element can be nitrogen etc.Catalyzer jet pipe can be U-shaped, S type or W type, needs to explain, being U-shaped when group catalyzer jet pipe number is 2, is S type when group catalyzer jet pipe number is 3.
According to a particular embodiment of the invention, catalyzer arm is arranged on the interlayer of heat accumulation type radiant tube.According to a particular embodiment of the invention, catalyst ejector part is arranged in the interlayer of heat accumulation type radiant tube.
Catalyzer arm is arranged at radiator tube interlayer effectively can prevent powder-material blocking catalyst jet pipe, can ensure that material can mix with catalyzer uniform contact after radiator tube is uniform simultaneously, ensure good reaction effect, can prevent catalyzer arm from wearing and tearing simultaneously, extend its work-ing life, reduce and change number of times.According to concrete example of the present invention, the number of muonic catalysis agent jet pipe can be determined according to the radiator tube number in every layer of heat accumulation type radiant tube, and then can make to be furnished with muonic catalysis agent jet pipe around every root heat accumulation type radiant tube.And then raising catalyzer adds uniformity coefficient, and reaction degree of being heated evenly.The catalyzer of particle diameter≤0.5mm is sprayed in coal charge layer equably by muonic catalysis agent jet pipe.Muonic catalysis agent jet pipe adopts the round tube of DN30-80, and catalyzer is blown in the muonic catalysis agent jet pipe of every layer by catalyzer supervisor.
According to concrete example of the present invention, the aperture of each catalyzer spray orifice 443 is 1/6 ~ 1/3 of muonic catalysis agent jet pipe caliber; Distance between adjacent two catalyzer spray orifices on muonic catalysis agent jet pipe is 2 ~ 8 times of catalyzer spray orifice aperture.According to a particular embodiment of the invention, the multiple catalyzer spray orifices 443 on the tube wall of each muonic catalysis agent jet pipe 442 are uniformly distributed and all down, and then prevent feed blocking catalyzer spray orifice.By controlling the caliber of above-mentioned muonic catalysis agent jet pipe, catalyzer spray orifice aperture, pitch of holes, and then control the amount and efficiency adding catalyzer, catalytic gasification reacts, and improves gasification efficiency.
According to concrete example of the present invention, the end that part is connected to described catalyzer supervisor is sent in described carrier gas.According to concrete example of the present invention, described carrier gas is sent part and is removably connected or be soldered to described catalyzer supervisor.
Thus, adopt above-mentioned catalyzer to add assembly supply catalyzer, catalyzer can be made to be scattered in equably in stove, with coal Homogeneous phase mixing.With directly spray into the reactor of catalyzer in prior art in reactor head compared with, catalyzer directly can be injected into gasification zone, can not affect the stream shape of coal in reactor coal ingress.
According to concrete example of the present invention, catalyzer arm is responsible for catalyzer on the one end be connected and is provided with variable valve, to adjust the inlet amount of catalyzer.
According to a particular embodiment of the invention, above-mentioned gasifying reactor can further include: feeding screw 50 and spiral slag off apparatus 60, and feeding screw is connected with described opening for feed, and described spiral slag off apparatus is connected with described slag-drip opening.Charging and deslagging efficiency can be improved further thus.
Embodiment 1
Para-bituminous coal granularity 1 ~ 5mm
1) radiator tube in gasifying reactor is the circular radiation pipe of DN200mm, radiator tube left and right between centers 300mm.Vertical centre spacing is 400mm.Laying tube layer position is 18 layers, reactor width 2.9m;
2) perforate of catalyzer jet pipe is directly 1/4 of catalyzer ejection passage, and on catalyzer jet pipe, perforate spacing is preferably direct 3 times of perforate;
3) particle diameter be the catalyzer of 0.5mm by catalyzer supervisor, arm and catalyzer jet pipe, spray into vapourizing furnace inside, with carbonaceous material Homogeneous phase mixing;
4) vapourizing furnace gasification temperature 1380 DEG C is controlled;
5) the vitreous state lime-ash produced is discharged after Quench by the deslagging spiral of bottom discharge mouth.
Gasification gas composition:
In describing the invention, it will be appreciated that, term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ", " thickness ", " on ", D score, " front ", " afterwards ", " left side ", " right side ", " vertically ", " level ", " top ", " end " " interior ", " outward ", " clockwise ", " counterclockwise ", " axis ", " radial direction ", orientation or the position relationship of the instruction such as " circumference " are based on orientation shown in the drawings or position relationship, only the present invention for convenience of description and simplified characterization, instead of indicate or imply that the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore limitation of the present invention can not be interpreted as.
In addition, term " first ", " second " only for describing object, and can not be interpreted as instruction or hint relative importance or imply the quantity indicating indicated technical characteristic.Thus, be limited with " first ", the feature of " second " can express or impliedly comprise one or more these features.In describing the invention, the implication of " multiple " is two or more, unless otherwise expressly limited specifically.
In the present invention, unless otherwise clearly defined and limited, the term such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or integral; Can be mechanical connection, also can be electrical connection; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals or the interaction relationship of two elements.For the ordinary skill in the art, above-mentioned term concrete meaning in the present invention can be understood as the case may be.
In the present invention, unless otherwise clearly defined and limited, fisrt feature second feature " on " or D score can be that the first and second features directly contact, or the first and second features are by intermediary indirect contact.And, fisrt feature second feature " on ", " top " and " above " but fisrt feature directly over second feature or oblique upper, or only represent that fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " below " and " below " can be fisrt feature immediately below second feature or tiltedly below, or only represent that fisrt feature level height is less than second feature.
In the description of this specification sheets, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means to describe in conjunction with this embodiment or example are contained at least one embodiment of the present invention or example.In this manual, to the schematic representation of above-mentioned term need not for be identical embodiment or example.And the specific features of description, structure, material or feature can combine in one or more embodiment in office or example in an appropriate manner.In addition, when not conflicting, the feature of the different embodiment described in this specification sheets or example and different embodiment or example can carry out combining and combining by those skilled in the art.
Although illustrate and describe embodiments of the invention above, be understandable that, above-described embodiment is exemplary, can not be interpreted as limitation of the present invention, and those of ordinary skill in the art can change above-described embodiment within the scope of the invention, revises, replace and modification.
Claims (8)
1. a gasifying reactor, is characterized in that, comprising:
Gasification agent nozzle, described gasification agent nozzle stretches to the top in described gasifying reactor by the roof of described gasifying reactor, the outlet side of described gasification agent nozzle tapered and cone the end down;
Heat accumulation type radiant tube, it is inner that described heat accumulation type radiant tube is arranged in described gasifying reactor, and arrange along the short transverse multilayer of described gasifying reactor, and every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction;
Catalyzer adds assembly, and described catalyzer adds assembly and comprises:
Catalyst hooper;
Catalyzer is responsible for, and described catalyzer supervisor is arranged on outside described gasifying reactor vertically; Described catalyzer supervisor is connected with described catalyst hooper;
Catalyzer arm, described catalyzer arm through described gasifying reactor sidewall and extend to the inside of described gasifying reactor, described catalyzer arm is responsible for described catalyzer and is connected;
One or more catalyst ejector part, described catalyst ejector part is arranged on described catalyzer arm, and it is inner to be positioned at described gasifying reactor,
Part is sent in carrier gas, and described carrier gas is sent part and is responsible for described catalyzer and is connected, and described carrier gas is sent part and is configured to be suitable for catalyzer to be blown into described gasifying reactor.
2. gasifying reactor according to claim 1, is characterized in that, described catalyzer arm is multiple, and the length direction be responsible for along described catalyzer is arranged parallel to each other,
Optionally, described catalyzer arm is responsible for perpendicular to described catalyzer,
Optionally, described catalyzer arm extends to the whole layer width of described heat accumulation type radiant tube layer.
3. gasifying reactor according to claim 1 and 2, it is characterized in that, described catalyst ejector part comprises catalyzer jet pipe and is arranged on the nozzle on described catalyzer jet pipe, and described nozzle is provided with variable valve, optionally, described catalyzer jet pipe is U-shaped, S type or W type jet pipe.
4. gasifying reactor according to claim 1 and 2, is characterized in that, described catalyst ejector part comprises catalyzer jet pipe, and the tube wall of described catalyzer jet pipe is provided with through hole, and optionally, described catalyzer jet pipe is U-shaped, S type or W type jet pipe.
5. the gasifying reactor according to any one of claim 1-4, is characterized in that, described catalyzer arm is arranged on the interlayer of described heat accumulation type radiant tube,
Optionally, described catalyst ejector part is arranged in the interlayer of described heat accumulation type radiant tube.
6. the gasifying reactor according to any one of claim 1-5, is characterized in that, the end that part is connected to described catalyzer supervisor is sent in described carrier gas.
7. the gasifying reactor according to any one of claim 1-6, is characterized in that, described carrier gas is sent part and removably connected or be soldered to described catalyzer supervisor.
8. gasifying reactor according to claim 1, is characterized in that, the outlet side of described gasification agent nozzle is tapered, and taper base angle is identical with the roof angle of inclination of described reactor.
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| CN106635174A (en) * | 2016-12-09 | 2017-05-10 | 中国科学院广州能源研究所 | Regenerative gasification device for high calorific value synthesis gas and gasification production method based on device |
| CN106681392A (en) * | 2016-12-01 | 2017-05-17 | 北京神雾环境能源科技集团股份有限公司 | Method and device for controlling temperatures of pyrolysis furnaces |
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