CN104498103A - Compound circulating fluidized bed gasification reaction device - Google Patents
Compound circulating fluidized bed gasification reaction device Download PDFInfo
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- CN104498103A CN104498103A CN201410853127.8A CN201410853127A CN104498103A CN 104498103 A CN104498103 A CN 104498103A CN 201410853127 A CN201410853127 A CN 201410853127A CN 104498103 A CN104498103 A CN 104498103A
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- air distribution
- circulating fluidized
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- 238000002309 gasification Methods 0.000 title claims abstract description 151
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 39
- 150000001875 compounds Chemical class 0.000 title abstract 4
- 239000000446 fuel Substances 0.000 claims abstract description 111
- 239000000843 powder Substances 0.000 claims abstract description 61
- 239000002245 particle Substances 0.000 claims abstract description 16
- 239000000463 material Substances 0.000 claims abstract description 14
- 239000002893 slag Substances 0.000 claims abstract description 7
- 239000010419 fine particle Substances 0.000 claims abstract description 6
- 238000009826 distribution Methods 0.000 claims description 57
- 239000000126 substance Substances 0.000 claims description 39
- 239000006200 vaporizer Substances 0.000 claims description 21
- 239000003795 chemical substances by application Substances 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 9
- 239000002826 coolant Substances 0.000 claims description 8
- 239000003507 refrigerant Substances 0.000 claims description 7
- 239000007921 spray Substances 0.000 claims description 5
- 230000007423 decrease Effects 0.000 claims description 4
- 239000011362 coarse particle Substances 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 8
- 229910052799 carbon Inorganic materials 0.000 abstract description 8
- 238000013461 design Methods 0.000 abstract description 5
- 238000007599 discharging Methods 0.000 abstract description 3
- 239000004449 solid propellant Substances 0.000 abstract description 3
- 239000003245 coal Substances 0.000 description 31
- 238000005516 engineering process Methods 0.000 description 22
- 239000007789 gas Substances 0.000 description 16
- 239000002956 ash Substances 0.000 description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 10
- 238000000034 method Methods 0.000 description 8
- 238000010586 diagram Methods 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 239000003077 lignite Substances 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 230000008018 melting Effects 0.000 description 4
- 238000002844 melting Methods 0.000 description 4
- 239000002817 coal dust Substances 0.000 description 3
- 238000005243 fluidization Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- 239000008188 pellet Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000003139 buffering effect Effects 0.000 description 2
- 235000011089 carbon dioxide Nutrition 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 230000002925 chemical effect Effects 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen(.) Chemical compound [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000007493 shaping process Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 238000012546 transfer 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
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
-
- 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
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
-
- 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
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
-
- 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
- C10J2300/0936—Coal fines for producing producer gas
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention provides a compound circulating fluidized bed gasification reaction device. The compound circulating fluidized bed gasification reaction device comprises a reactor body, a multistage cyclone separator, a particle fuel feeding system, a powder fuel feeding system, a central jet flow gasification burner nozzle and a material returning system, wherein the outlet of the reactor is connected with a primary cyclone separator; the primary cyclone separator is connected with a secondary cyclone separator; crude particles separated by the primary cyclone separator are returned to a gasification furnace body by virtue of the material returning system; fine particles separated by the secondary cyclone separator enter the central jet flow gasification burner nozzle by virtue of the powder fuel feeding system and are finally sprayed to the gasification furnace body. A circulating fluidized bed reactor is used as a gas reaction body; the slag is continuously discharged by gasifying at a medium-high temperature; by virtue of application of high-temperature jet flow two-stage grading gasification, the carbon conversion rate and the cold gas efficiency are increased; a simplified slag discharging device is combined with the design of an air distributing plate; the operation stability and the running stability are improved; the compound circulating fluidized bed gasification reaction device is suitable for gasifying and converting various carbon-containing solid fuels and has large-scale popularization and application prospects.
Description
Technical field
The present invention relates to a kind of combined type circulating fluidized-bed gasification reaction unit, belong to Coal (syngas) polygeneration technical field.
Background technology
Gasification technology for the production of clean energy and product is long-standing, can trace back to the Britain of 18 th century later the earliest.Early stage vaporous form utilizes local coal resources to produce " domestic gas (Town Gas) ".Modern gasification technology starts from World War II in earlier stage, and is being developed during the Second World War.The oil supply of Germany was cut off at that time, and needing badly looks for another way carrys out production and transport fuel voluntarily, and therefore, increasing advanced gasification technology is researched and developed during this period.After this, husky rope (Sasol) company in South Africa takes the lead in the gasification derived product utilizing the gasification technology commercialization of production on a large scale, have price competitiveness, thus has established the basis of modern gasification industry.
Now, basis in early days achieves important breakthrough to advanced gasification technology.Fuel flexibility raising, vaporization ability and scale increase, the application of new technique impels gasification technology to obtain larger breakthrough.The application of advanced gasification technology and popularization contribute to the problem solving the aspects such as social economy, energy security and environment protection.Meanwhile, because Research Emphasis is different, gasification technology also differentiates dissimilar, and a part is intended to reduce costs by integrating, another part is then devoted to development of small-scale, modular vapourizing furnace.Although applying of gasification technology still faces many difficulties, this circumstances makes moderate progress in the recent period, particularly puts into practice in the demonstration of China, fully illustrates gasification technology utilizing domestic Energy conversion and becomes the huge advantage had in commerical prod.
The low-rank coal aboundresources such as China's brown coal, account for the whole nation and verify 50% of coal reserves, the low-rank coal such as brown coal have high ash, high water and high-sulfur (" three is high "), and the feature such as part high ash melting point, existing Coal Gasification Technology is mainly air flow bed coal water slurry gasification, Dry Feeding Entrain Bed Coal Gasification and the gasification of fixed bed broken coal, from the angle analysis of gasification technology, air flow bed coal water slurry gasification requires higher to the slurryability of coal, the high-moisture characteristic of brown coal cannot meet Pulping conditions, Dry Feeding Entrain Bed Coal Gasification Technology needs coal to make coal dust, and coal dust total water content requires < 2%, high water brown coal dehydration cost and energy consumption huge, and entrained flow gasification general requirement ash fusion point is unsuitable too high, otherwise the running costs such as slag tap oxygen consumption increase.Fixed bed gasification technology adopts broken coal or type coal gasification technology, modernization big machinery is mined and the particulate coal productive rate of low strength moor coal is originally declined greatly, the a large amount of fine coal of output is not suitable for fixed bed gasification, need machine-shaping, energy consumption is huge, and the particle fraction that output raw coal can be directly used in gasification is about 10%, and fixed bed gasification technology after-treatment system is responsible for, coal tar extraction and isolation difficulty, environmental issue is given prominence to.According to current gasification technology present situation, the robust techniques that ciculation fluidized bed gasification technology there is no long-period stable operation is at present available, and portion of techniques bottleneck needs to research and develop breakthrough further.
Summary of the invention
The technical problem to be solved in the present invention is to provide that a kind of operational condition is gentle, gasification efficiency is high, safeguard and simple, with low cost be suitable for low order coal gasification reactor, thus fills up air flow bed and fixed bed cannot gasify the technological gap of " three high coals ".
In order to solve the problems of the technologies described above, technical scheme of the present invention is to provide a kind of combined type circulating fluidized-bed gasification reaction unit, it is characterized in that: by reactor body, multi-cyclone, granular fuel feeds system, powder fuel feeds system, central jet gasification burner tip and material return system form;
Reactor body comprises vapourizing furnace body, and reactor outlet is located at vapourizing furnace bodies top, and vapourizing furnace body bottom portion is provided with center scum pipe, and air distribution plate, with being located in above central row slag pipe, is vaporized chemical distributing chamber below air distribution plate; Be provided with central jet gasification burner tip in the scum pipe of center, below the scum pipe of center, be provided with gasification agent inlet; Vapourizing furnace body is divided into upper and lower two stage gasification room, and upper and lower two stage gasification room is connected by taper reducing section, and epimere vaporizer lower end is provided with two sections of gasification burner tip rooms, below taper reducing section, connects granular fuel feed system and material return system above air distribution plate;
Multi-cyclone is at least two stage cyclone separator series connection, and reactor outlet is connected with primary cyclone, and primary cyclone outlet is connected with secondary cyclone; The coarse particles separated through primary cyclone returns vapourizing furnace body hypomere vaporizer by material return system, the fine particle separated through secondary cyclone feeds system by powder fuel and enters central jet gasification burner tip, finally sprays into vapourizing furnace body.
Preferably, scum pipe top, described center is bell-mouth structure of air, and described air distribution plate is pyramidal structure, and center scum pipe flared end is connected with air distribution plate necking end; Central jet gasification burner tip, air distribution plate and center scum pipe are coaxially arranged.
Preferably, the particle size range 0 ~ 10mm of described granular fuel, accounts for 60% ~ 90% of total amount of fuel; Powder fuel particle size range 10 ~ 200 μm, accounts for 10% ~ 40% of total amount of fuel.
Preferably, described epimere vaporizer diameter D1 is greater than hypomere vaporizer diameter D2, both ratio range D1/D2=1.1 ~ 3.
Preferably, described granular fuel feeds system and comprises fuel bunker and fuel to dipleg, and fuel bunker is connected with the hypomere vaporizer of vapourizing furnace body to dipleg by fuel.
Preferably, described material return system comprises the first material-returning device, described primary cyclone is connected with the first material-returning device by a cycle dipleg, first material-returning device is connected with the second material-returning device by revert pipe, and the second material-returning device connects the hypomere vaporizer of described vapourizing furnace body by feed back leg.
Preferably, described powder fuel feeds system and comprises powder fuel storehouse, be provided with two bottom described secondary cyclone and screw off dipleg, two screw off dipleg connects powder fuel storehouse, dust-removal system is connected with powder fuel storehouse, powder fuel connects powder fuel storehouse to batch can by powder fuel lock hopper, and powder fuel is connected with described central jet gasification burner tip by powder fuel entrance to batch can.
Preferably, described central jet gasification burner tip comprises coaxial powder fuel passage, vaporized chemical passage, refrigerant admission passage and the coolant outlet passage arranged from inside to outside, and described powder fuel passes through powder fuel entrance and powder fuel expanding channels to batch can; A knuckle α is provided with, α scope 90 ° ~ 150 ° in the middle part of described central jet gasification burner tip.
Preferably, described air distribution plate is communicated by the air distribution plate vaporized chemical spout be located on air distribution plate with vaporized chemical distributing chamber, and described vaporized chemical distributing chamber connects gasification agent inlet pipe; Described air distribution plate band cooling system; Described air distribution plate is evenly provided with 5 ~ 30 circle sieve aperture spouts, often circle sieve aperture spout quantity is equal, and often enclose sieve aperture nozzle diameter and successively decrease along air distribution plate radial direction, the sieve aperture nozzle diameter near center scum pipe is minimum, is provided with sieve aperture baffle plate below sieve aperture spout.
Preferably, described vaporized chemical enters reactor body from described central jet gasification burner tip, center scum pipe, air distribution plate and two sections of gasification burner tip rooms, it is 20% ~ 80% that the vaporized chemical entering reactor body from central jet gasification burner tip accounts for all vaporized chemical ratios, central jet gasification burner tip upper end spout vaporized chemical flow velocity 8 ~ 30m/s.
Stable and reliable operation of the present invention, be easy to maximize amplify, environmental protection and energy saving, compared to existing technology, the present invention has following beneficial effect:
(1) adopt two-part circulating fluidized bed as the main device of gasification reaction, the introducing of central jet gasification burner tip revolutionizes the basic concept of conventional recycle fluidized-bed gasification, fuel is extended to powder fuel, and overall circulating fluidized bed vaporising fuel adaptability improves greatly;
(2) adopt the design of central jet gasification burner tip, one section of central jet district temperature in circle fluidized-bed gasification furnace improved, giving full play to heat output provides needed for periphery gasification, gasification rate improves, integrated gasification speed of response improves, and efficiency of carbon conversion improves, and cold gas efficiency improves;
(3) flying dust and thin grey recycle burning is adopted, and fired again by central jet gasification burner tip, ensure that efficient burning and the gasification of fine particle fuel, the unburned carbon in flue dust produced in ciculation fluidized bed gasification process is declined greatly, and the thick solid impurity particle of formation of reuniting in high-temperature zone, lime-ash treating processes simplifies greatly;
(4) low velocity fluidization speed in adopting, compared with melting bubbling bed apparent velocity ~ 1m/s conventional in gather qi together with existing ash, flow velocity improves can make more much particles participate in fluidisation, gas-particle two-phase Mass and heat transfer accelerates, improve gasification reaction speed, make reactor temperature distribution and material distribution more evenly, be convenient to set up stable bed.
The present invention adopts two-part to gasify and central jet gasification combines, circulating fluid bed reactor is adopted to be gasification reaction body, in employing, high-temperature gasification realizes continuous discharging slag, adopt high temp jet two-part classification gasification, solve existing fluidized-bed gasification reaction unit efficiency of carbon conversion low, the problems such as the high and lime-ash processing cost of system energy efficiency is high, reach the object improving efficiency of carbon conversion and cold gas efficiency, the slag discharging device simplified combines with air distribution plate design, improve operation and operation stability, the gasification being suitable for all kinds of carbonic solid fuels transforms, and effectively can decompose the larger molecular organicses such as tar, rear system synthesis gas purifying dust-collecting process simplifies greatly, effective gas productive rate improves greatly, equipment operation and maintenance cost reduces greatly, there is large-scale promotion application prospect.
Accompanying drawing explanation
Fig. 1 is combined type circulating fluidized-bed gasification reaction unit schematic diagram;
Fig. 2 is reactor body schematic diagram;
Fig. 3 is air distribution plate band cooling system schematic diagram;
Jet gasification burner tip front-end architecture schematic diagram centered by Fig. 4;
Fig. 5 is air distributor structure schematic diagram;
Jet gasification principle schematic diagram centered by Fig. 6;
Description of reference numerals
1-vapourizing furnace body; 2-primary cyclone; 3-secondary cyclone; 4-fuel bunker; 5-fuel is to dipleg; 6-feed back leg; 7-air distribution plate; 8-central jet gasification burner tip; 9-vaporized chemical distributing chamber; 10-gasification agent inlet pipe; 11-center scum pipe gasification agent inlet; 12-bis-sections of gasification burner tip rooms; 13-second material-returning device; 14-revert pipe; 15-first material-returning device; 16-bis-screws off dipleg; 17-mono-cycle dipleg; 18-reactor outlet; 19-syngas outlet pipe; 20-mono-screw outlet pipe; 21-bis-screw outlet; 22-dust-removal system; 23-powder fuel storehouse; 24-powder fuel lock hopper; 25-powder fuel is to batch can; 26-powder fuel conveying gas; 27-lime-ash buffering cooling tank; 28-powder fuel entrance; 29a, 29b-refrigerant import and export; 30-gasification agent inlet; 31-vaporized chemical passage; 32-powder fuel passage; 33-refrigerant admission passage; 34-coolant outlet passage; 35-air distribution plate vaporized chemical spout; 36-cooling jacket; 37-circular channel shower nozzle; 38-centre channel shower nozzle; 39-air distribution plate coolant entrance; 40-air distribution plate coolant outlet; 41-center scum pipe; 42-sieve aperture spout; 43-sieve aperture baffle plate.
Embodiment
For making the present invention become apparent, hereby with a preferred embodiment, and accompanying drawing is coordinated to be described in detail below.
Fig. 1 is combined type circulating fluidized-bed gasification reaction unit schematic diagram provided by the invention, described combined type circulating fluidized-bed gasification reaction unit by reactor body, multi-cyclone, granular fuel feeds system, powder fuel feeds system, central jet gasification burner tip and material return system etc. form.
Reactor body is made up of vapourizing furnace body 1, reactor outlet 18, air distribution plate 7, vaporized chemical distributing chamber 9, two sections of major partss such as gasification burner tip room 12, center scum pipe 41.Reactor outlet 18 is located at vapourizing furnace body 1 top, air distribution plate 7 and center scum pipe 41 is provided with bottom vapourizing furnace body 1, center scum pipe 41 top is a bell-mouth structure of air, air distribution plate 7 is pyramidal structure, center scum pipe flared end is connected with air distribution plate 7 necking end, is vaporized chemical distributing chamber 9 below air distribution plate 7.Central jet gasification burner tip 8 is provided with in the scum pipe of center, central jet gasification burner tip 8, air distribution plate 7 and center scum pipe are coaxially arranged, be provided with center scum pipe gasification agent inlet 11 below the scum pipe of center, bottom the scum pipe of center, be provided with lime-ash buffering cooling tank 27.
Vapourizing furnace body 1 is divided into upper and lower two stage gasification room, vapourizing furnace epimere vaporizer diameter D
1be greater than hypomere vaporizer diameter D
2, both ratio range D
1/ D
2=1.1 ~ 3, preferable range D
1/ D
2=1.6 ~ 2.4.Be provided with a taper reducing section in the middle part of vapourizing furnace body 1, upper and lower two stage gasification room is connected by taper reducing section.Be provided with two sections of gasification burner tip rooms 12 above epimere vaporizer lower end, taper reducing section, ignition oven burner and two sections of gasification burner tips can be installed.Be provided with granular fuel below taper reducing section, above air distribution plate 7 and feed system and material return system, both are symmetrically arranged in vapourizing furnace body circumference, and granular fuel is all positioned at above air distribution plate 7 to entrance and feedback outlet.
Multi-cyclone can carry out series-parallel connection setting, and namely carry out shunting to synthetic gas and formed in parallel, multi-cyclone is established in each bypass, is the series connection of two stage cyclone separator in the present embodiment.Reactor outlet 18 is connected with primary cyclone 2 by syngas outlet pipe 19, and primary cyclone 2 is connected with secondary cyclone 3 by a screw outlet pipe 20, and secondary cyclone 3 top is provided with two screw outlets 21.
Granular fuel feeds system and comprises fuel bunker 4 and fuel to dipleg 5, and fuel bunker 4 is connected with the hypomere vaporizer of vapourizing furnace body 1 to dipleg 5 by fuel.
Powder fuel feeds system and comprises powder fuel storehouse 23, dust-removal system 22 is connected with powder fuel storehouse 23, powder fuel connects powder fuel storehouse 23 to batch can 25 by powder fuel lock hopper 24, and powder fuel is connected with central jet gasification burner tip 8 by powder fuel entrance 28 to batch can 25.
Material return system comprises the first material-returning device 15, primary cyclone 2 is connected with the first material-returning device 15 by a cycle dipleg 17, first material-returning device 15 is connected with the second material-returning device 13 by revert pipe 14, and the second material-returning device 13 connects the hypomere vaporizer of vapourizing furnace body 1 by feed back leg 6.
Be provided with two bottom secondary cyclone 3 and screw off dipleg 16, two screw off dipleg 16 can connect powder fuel storehouse 23, two and screw off dipleg 16 also directly can connect vapourizing furnace body 1 hypomere vaporizer by feed back leg 6.
Composition graphs 2 ~ Fig. 4, central jet gasification burner tip 8 adopts telescopic design, is provided with jacketed type cooling system, and the refrigerants such as water can be adopted to cool.Centre channel is powder fuel passage 32, and its top is provided with centre channel shower nozzle 38, and bottom is provided with powder fuel entrance 28; Circular channel is vaporized chemical passage 31, and its top is provided with circular channel shower nozzle 37, and bottom is provided with gasification agent inlet 30; Outermost is cooling jacket 36, comprises refrigerant admission passage 33 and coolant outlet passage 34, is respectively equipped with refrigerant import and export 29a, 29b bottom it.Gasification burner tip upper end spout logistics flow velocity 8 ~ 35m/s, preferred value 15m/s.Centre channel passes into coal dust and the rare gas element such as nitrogen or carbonic acid gas can be adopted to carry.
Air distribution plate 7 is communicated by the air distribution plate vaporized chemical spout 35 be located on air distribution plate with vaporized chemical distributing chamber 9, and vaporized chemical distributing chamber 9 is connected with gasification agent inlet pipe 10.Composition graphs 3, air distribution plate 7 is with cooling system, and in Fig. 3,39 is air distribution plate coolant entrance, and 40 is air distribution plate coolant outlet.Composition graphs 5, air distribution plate vaporized chemical spout 35 is arranged along air distribution plate 7 even circumferential, be provided with 5 ~ 30 circle sieve aperture spouts 42, often enclose sieve aperture spout quantity equal, often enclose sieve aperture nozzle diameter and successively decrease along air distribution plate radial direction, the sieve aperture nozzle diameter near center scum pipe is minimum, controlling vaporized chemical from air distribution plate sieve aperture spout ejection flow rates is 0.5 ~ 5m/s, preferred value 0.8 ~ 3m/s, in order to prevent lime-ash from falling into air distribution plate cavity, is provided with sieve aperture baffle plate 43 below sieve aperture spout.
Air distribution plate is pyramidal structure, bell angle theta angular range 30 ° ~ 120 °, preferred value 30 ° ~ 60 °.Scum pipe epimere enlarging angle, center β angular range 10 ~ 45 °, preferred value 15 ° ~ 30 °.A knuckle α is provided with, α angular range 90 ° ~ 150 °, preferable range 120 ° ~ 135 ° in the middle part of central jet gasification burner tip.Two sections of gasification burner tip room central axis and horizontal plane shape have angle μ, angle μ angular range 90 ° ~ 150 °, preferred value 120 °.Two sections of gasification burner tip rooms 12 are evenly arranged along the simplified circumference same level of reactor, two sections of gasification burner tip room number scopes 1 ~ 8, preferably 2 ~ 4, two sections of gasification burner tip room central axis and horizontal plane shape have angle μ, angle μ angular range 90 ° ~ 150 °, preferred value 120 °.In the middle of vapourizing furnace body, the bell angle η scope of taper reducing section is 15 ° ~ 60 °, preferably 30 ° ~ 45 °.
The fuel amount of feeding W
1with feed back amount W
2ratio be called circulation ratio, i.e. W
2/ W
1, controlled circulation multiplying power scope is 20 ~ 80.Circulation ratio is regulated by bed apparent velocity, and apparent velocity has reacted air-flow cross sectional flow rate in reactor, and it ranges preferably from 2 ~ 10m/s, is preferably 3 ~ 5m/s.Gasifying reactor service temperature is 800 ~ 1200 DEG C, according to used fuel ash melting characteristic, and working pressure scope 0 ~ 6.0MPa.Vaporized chemical control speed 1 ~ 15m/s that two sections of gasification burner tip rooms spray into, preferable range 2 ~ 8m/s.
Fuel is based on solid granulates, reactor is entered by high-pressure delivery feed-type, particle size range 0 ~ the 20mm of fuel pellet, preferably 0 ~ 10mm, account for 60 ~ 90% of total amount of fuel, residue 10 ~ 40% adopts powder fuel form to send into system by powder fuel and sends into vapourizing furnace to central jet gasification burner tip, and powder fuel particle diameter is preferably 10 ~ 200 μm, preferable particle size scope 40 ~ 100 μm, can select N
2, CO
2or other one or more mixed gas delivery.
Composition graphs 6, fuel of the present invention comprises all carbonic solid fuels, comprises biomass, coal, refinery coke, blue charcoal, coal gangue and composition thereof.Grain breakage is got the raw materials ready to below 20mm fuel bunker 4, fluidized-bed reactor is sent into by fuel area density leg 5, powder fuel is adopted to carry gas 26 to send into central jet gasification burner tip 8 after feeding system by the fine particle of screening by powder fuel, vaporized chemical is respectively by center scum pipe 41, central jet gasification burner tip 8 vaporized chemical passage 31 and the vaporized chemical spout 35 set by air distribution plate 7 send into reactor, first at the indoor generation burning of gasified and gasification reaction, central jet gasification produces about 1300 DEG C of high temperature, powder fuel melting is reunited, heat radiation is used for gasification to periphery, vaporized chemical carries fuel pellet and forms fluidization, air-flow carries partial particulate and upwards flows into epimere vaporizer, second gasification reaction is there is under the vaporized chemical effect that two sections of burner rooms 12 spray into, and set up stable bed, synthetic gas is discharged by reactor head outlet 18, and be entrained with the fuel pellet of the non-complete reaction of part, under the effect of primary cyclone 2 and secondary cyclone 3, particle is separated, respectively by feed back leg 16 and 17 to material-returning device, after coarse particles is separated by the first cyclonic separator 2, successively through decline dipleg 14, material-returning device 13 and feed back leg 6 directly return vapourizing furnace 1, fine particle returns to powder fuel storehouse 23 after being separated by the second cyclonic separator 3, form cycle gasification, reach higher circulation ratio and gasification efficiency, coal combustiblematerials is thoroughly transformed.
In gasification reactor apparatus, the equipment such as gasifying reactor 1, one/secondary cyclone 2,3 all adopts refractory liner structure, and side towards the fire adopts abrasionproof refractory liner.
Vaporized chemical can select water vapor, oxygen, oxygen-rich air (O
2volumetric concentration > 21%) and carbonic acid gas and mixed gas thereof, oxygen does not need to reach certain flow as oxygenant and fuel occurs to burn and gasification reaction.Major part vaporized chemical is sent into from central jet gasification burner tip 8, air distribution plate 7 and center scum pipe 41, and all the other vaporized chemicals spray into gasifying reactor by two sections of gasification burner tip rooms 12.
For the combined type circulating fluidized-bed gasification reaction unit of a day output 2000 tons of brown coal.The coal data of bunker coal is shown in Table 1.The design variable of gasification reactor apparatus is as follows:
Working pressure: 4.0MPaG;
Service temperature: 1160 DEG C;
Vaporized chemical: pure oxygen and water vapor;
Broken coal fuel particle diameter: 0 ~ 10mm, median size 6mm, total mass accounting 80%;
Pulverized coal fuel particle diameter: 0 ~ 200 μm, median size 65 μm, total mass accounting 15%, adopts N
2conveying;
Circulating ash accounts for powder fuel and feeds total amount 5%;
Structure of reactor: hypomere vaporizer internal diameter 1100mm, high 7500mm, epimere vaporizer internal diameter 1750mm, high 16800mm, conical section reducing angle 45 °;
Circulation ratio: 25;
Vaporized chemical distributes: central jet gasification burner tip accounts for 50%, air distribution plate 25%, two sections of burner rooms 15%, center scum pipe 10%;
Deslagging temperature: 1000 DEG C;
Cross section apparent velocity: ~ 3.5m/s in reactor.
Table 1 bunker coal coal analysis data
Gasification reaction exiting syngas predominant gas forms:
CO：45.12；H
2：38.08；CH
4：4.32；CO
2：4.59；H
2O：5.75；N
2：1.86
Synthetic gas flow: 6870kmol/h;
Synthetic gas temperature: 1028 DEG C;
Water vapor consumes: 11867kg/h;
Oxygen depletion: 28534kg/h;
Nitrogen consumes: 450Nm
3/ h;
Domestic and international similar technique representative art index contrast situation is shown in Table 2.
Table 2 fluidized-bed gasification reaction technology index contrasts
From the technical indicator centering of table 2, can draw, combined type circulating fluidized-bed gasification reaction unit described in patent of the present invention on the consumption indicators such as oxygen depletion, water vapor consumption due to domestic and international similar technique, efficiency of carbon conversion exceeds more than about 10 percentage points, service temperature is moderate, achieve fine coal and broken coal feed vaporization simultaneously, efficiency of carbon conversion reaches more than 99%, produces coal ash and can be used as building materials utilization and harmless treatment.
In sum, patent of the present invention has obvious technological innovation advantage, is applicable to the large-scale promotion application of the trans-utilizations such as fuel gasification.
Claims (10)
1. a combined type circulating fluidized-bed gasification reaction unit, is characterized in that: by reactor body, multi-cyclone, granular fuel feeds system, powder fuel feeds system, central jet gasification burner tip and material return system form;
Reactor body comprises vapourizing furnace body (1), reactor outlet (18) is located at vapourizing furnace body (1) top, vapourizing furnace body (1) bottom is provided with center scum pipe (41), air distribution plate (7) is with being located in central row slag pipe (41) top, and air distribution plate (7) below is vaporized chemical distributing chamber (9); Be provided with central jet gasification burner tip (8) in center scum pipe (41), center scum pipe (41) below is provided with gasification agent inlet; Vapourizing furnace body (1) is divided into upper and lower two stage gasification room, upper and lower two stage gasification room is connected by taper reducing section, epimere vaporizer lower end is provided with two sections of gasification burner tip rooms (12), connects granular fuel and feed system and material return system below taper reducing section, above air distribution plate (7);
Multi-cyclone is at least two stage cyclone separator series connection, and reactor outlet (18) is connected with primary cyclone (2), and primary cyclone (2) outlet is connected with secondary cyclone (3); The coarse particles separated through primary cyclone (2) returns vapourizing furnace body (1) hypomere vaporizer by material return system, the fine particle separated through secondary cyclone (3) feeds system by powder fuel and enters central jet gasification burner tip (8), finally sprays into vapourizing furnace body (1).
2. a kind of combined type circulating fluidized-bed gasification reaction unit as claimed in claim 1, it is characterized in that: scum pipe (41) top, described center is bell-mouth structure of air, described air distribution plate (7) is pyramidal structure, and center scum pipe (41) flared end is connected with air distribution plate (7) necking end; Central jet gasification burner tip (8), air distribution plate (7) and center scum pipe (41) are coaxially arranged.
3. a kind of combined type circulating fluidized-bed gasification reaction unit as claimed in claim 1, is characterized in that: the particle size range 0 ~ 10mm of described granular fuel, accounts for 60% ~ 90% of total amount of fuel; Powder fuel particle size range 10 ~ 200 μm, accounts for 10% ~ 40% of total amount of fuel.
4. a kind of combined type circulating fluidized-bed gasification reaction unit as claimed in claim 1, is characterized in that: described epimere vaporizer diameter D1 is greater than hypomere vaporizer diameter D2, both ratio range D1/D2=1.1 ~ 3.
5. a kind of combined type circulating fluidized-bed gasification reaction unit as claimed in claim 1, it is characterized in that: described granular fuel feeds system and comprises fuel bunker (4) and fuel to dipleg (5), and fuel bunker (4) is connected to the hypomere vaporizer of dipleg (5) with vapourizing furnace body (1) by fuel.
6. a kind of combined type circulating fluidized-bed gasification reaction unit as claimed in claim 1, it is characterized in that: described material return system comprises the first material-returning device (15), described primary cyclone (2) is connected with the first material-returning device (15) by a cycle dipleg (17), first material-returning device (15) is connected with the second material-returning device (13) by revert pipe (14), and the second material-returning device (13) connects the hypomere vaporizer of described vapourizing furnace body (1) by feed back leg (6).
7. a kind of combined type circulating fluidized-bed gasification reaction unit as claimed in claim 1, it is characterized in that: described powder fuel feeds system and comprises powder fuel storehouse (23), described secondary cyclone (3) bottom is provided with two and screws off dipleg (16), two screw off dipleg (16) connects powder fuel storehouse (23), dust-removal system (22) is connected with powder fuel storehouse (23), powder fuel connects powder fuel storehouse (23) to batch can (25) by powder fuel lock hopper (24), powder fuel is connected with described central jet gasification burner tip (8) by powder fuel entrance (28) to batch can (25).
8. a kind of combined type circulating fluidized-bed gasification reaction unit as claimed in claim 7, it is characterized in that: described central jet gasification burner tip (8) comprises coaxial powder fuel passage (32), vaporized chemical passage (31), refrigerant admission passage (33) and the coolant outlet passage (34) arranged from inside to outside, and described powder fuel is connected with powder fuel passage (32) by powder fuel entrance (28) to batch can (25); Described central jet gasification burner tip (8) middle part is provided with a knuckle α, α scope 90 ° ~ 150 °.
9. a kind of combined type circulating fluidized-bed gasification reaction unit as claimed in claim 1, it is characterized in that: described air distribution plate (7) is communicated by the air distribution plate vaporized chemical spout (35) be located on air distribution plate with vaporized chemical distributing chamber (9), described vaporized chemical distributing chamber (9) connects gasification agent inlet pipe (10); Described air distribution plate (7) band cooling system; Described air distribution plate (7) is evenly provided with 5 ~ 30 circles sieve aperture spout (42), often enclose sieve aperture spout (42) quantity equal, often enclose sieve aperture spout (42) diameter to successively decrease along air distribution plate radial direction, sieve aperture spout (42) diameter near center scum pipe (41) is minimum, and sieve aperture spout (42) below is provided with sieve aperture baffle plate (43).
10. a kind of combined type circulating fluidized-bed gasification reaction unit as claimed in claim 8, it is characterized in that: vaporized chemical enters reactor body from described central jet gasification burner tip (8), center scum pipe (41), air distribution plate (7) and two sections of gasification burner tip rooms (12), it is 20% ~ 80% that the vaporized chemical entering reactor body from central jet gasification burner tip (8) accounts for all vaporized chemical ratios, central jet gasification burner tip (8) upper end spout vaporized chemical flow velocity 8 ~ 30m/s.
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| CN104862011A (en) * | 2015-05-25 | 2015-08-26 | 山东百川同创能源有限公司 | Pyrolysis gasification system for biomass solid waste and hazardous waste |
| CN105222129A (en) * | 2015-11-05 | 2016-01-06 | 东南大学 | A kind of coal-fired burning chemistry chains separation of C O of the pure oxygen gasification that is coupled 2method |
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