CN201010630Y - Fluid bed powder coal gasifying reactor - Google Patents
Fluid bed powder coal gasifying reactor Download PDFInfo
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- CN201010630Y CN201010630Y CN 200620128241 CN200620128241U CN201010630Y CN 201010630 Y CN201010630 Y CN 201010630Y CN 200620128241 CN200620128241 CN 200620128241 CN 200620128241 U CN200620128241 U CN 200620128241U CN 201010630 Y CN201010630 Y CN 201010630Y
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- 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]
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Abstract
The utility model belongs to the filed of fluidized bed powdered coal gasifying reactor. The reactor is composed of two sections of double-fire-bed sprouted fluidized beds, a dense-phase reaction section with central sprouting pipe of the sprouted fluidized bed is provided at the bottom of the reactor and used for agglomeration and selectively discharging of ash; a dilute-phase post-reaction adjusting section with a secondary gasifying agent feeder is provided at the upper part of the reactor and used for converting unreacted dust through nozzles with certain amount and angle and adjusting gas composition and load; a radial type cooler is provided at the outlet of the reactor and used for prevent the overheat of the byproduct steam. The utility model adopts an inner lined corundum layer and a polycrystalline fiber plate double-layer heat insulating wall structure as well as a water jacket cold wall outer shell structure to both improve the heat efficiency of the device and meet the anti-heat shock requirements under the prerequisite of assuring the safety and reliability of the device; and is a practical powdered coal gasifying reactor.
Description
Technical field
The utility model relates to a kind of fluidized-bed coal dust equipment for gasification, especially for the reactor of sulfuration bed coal gasification reaction production.
Background technology
Fluid bed powder coal gasification equipment is a kind of known technology, industrialized have Winkler (Winkler) and through the improvement after grace, high temperature Winkler (HTW) and circulating fluidized bed (Lurgi) technology and equipment thereof.Although solved some problems such as gas distribution inequality in the early stage fluidized-bed, easily slagging scorification, top radiant boiler failure rate height, efficiency of carbon conversion are low, improved the operation factor and the reliability of device to a certain extent with (Winkler) process technology equipment after the improvement.But still have the outstanding problem of following several respects: at first, the coal adaptability of this equipment is poor, can only adapt to the coal of the low metamorphic grades such as brown coal, long-flame coal of some high reaction activities, low coking, slagging scorification; Secondly, because this equipment reaction temperature can not be too high, cause CH in the gas
4And CO
2Content is higher, and it is unfavorable that synthetic gas is produced; Once more, owing to move behind this device dust, environment is caused certain pollution; At last, because this equipment pressure is higher, counter investment is higher, and input-output are unreasonable.
Summary of the invention
Problem of the present utility model is to improve the adaptability of fluid bed powder coal gasification reactor coal, efficiency of carbon conversion and effective pneumatolytic part, widens fluid bed powder coal gasification reactor feedstocks coal scope, reduces CH in the gas
4And CO
2Content, the minimizing dust is carried secretly and is polluted, and a kind of fluid bed powder coal gasification reactor is provided.
For reaching its above-mentioned purpose, primary theme of the present utility model is a kind of fluid bed powder coal gasification reactor, and this reactor is made of two sections double fire layer spouted fluidized beds that have radiant cooler.
This reactor is characterized in that: adopt the up big and down small concentric tube bodily form formula with middle transition (II), and cylindrical shell has cold and hot wall composite structure, form the water jacket cooling channel between wherein inside and outside cylindrical shell, inner barrel is cooled off, and the inner barrel inwall is lined with adiabatic sealing coat and high temperature resistant wear-resistant lining.
Its feature of this reactor also is: the bottom is the spouted fluidized bed emulsion zone conversion zone (I) with central spouted pipe, implements the reunion and the selectivity of ash and discharges; Top is only to have the freeboard of fluidized bed postreaction of lacking a second gasification agent charging to adjust section (III), finishes the conversion of unreacted dust by the nozzle of some amount, angle, adjusts gas composition and load simultaneously; And be provided with radiant cooler in outlet, be used for the overheated of byproduct steam.
Another theme of the present utility model is a kind of method and apparatus of fluid bed powder coal gasification, in this method, comprise at least one cover coal system device, feed coal enters reactor by at least one coal filling hole on vaporized chemical sparger fluidising chamber (B) top of emulsion zone conversion zone (I) by this system, vaporized chemical is respectively by at least one nozzle, select ash discharge chamber's endless tube inlet, the spouted tube inlet in center and at least one secondary air inlet enter reactor, and feed coal and vaporized chemical experience two sections double fire layer (I in reactor, III) reaction and cooling (5A) back are derived by the top-side outlet.The reunion ash that forms in the reactor is discharged by selectivity ash discharge chamber (A) and after cooling, collection and decompression.The dust-laden coal gas that reactor head derives at first enters recovery of heat, dry type pottery fly-ash separator and washing tower and sends system after the high-temperature cyclone dust extractor dedusting, the dust of high-temperature cyclone dust extractor is further reacted by reactor return port Returning reactor, and the fine dust of dry type pottery fly-ash separator is discharged after cooling, collection and decompression.
The feature of aforesaid method and equipment is: owing to adopt two sections spouted fluidized bed coal gasifications of double fire layer reactor in close phase reaction section, the characteristic of utilizing ash to reunite, be provided with a central nozzle according to spouted principle at the bed central area and produce the localized hyperthermia district, make the temperature of ash reach the reunion that grey molten accumulation carries out ash; Method with general fluidized-bed adopts the coal conversion process that on every side form lesser temps of orifice gas distributed architecture at spouted pipe, has avoided the destruction fluidizing phenomenons such as slagging scorification of bed; Utilize the severe difference of different carbon residue slags then, (A) is provided with the structural part of a selectivity ash discharge in the bottom.The control of implementing bed drain purge and carbon residue by the speed of adjusting air inlet is carried out the selectivity ash discharge and is reduced remaining carbon.By this kind structure the adaptability of coal is increased greatly, can expand to stock number bigger and distribute bituminous coal, greedy coal, greedy lean coal, hard coal even coke powder and refinery coke widely by the raw material of low metamorphic grade.
Another feature of aforesaid method and equipment is: introduce the second gasification agent at the vapourizing furnace middle part, produce the reaction of second fire bed and adjust section, will go into the CH in the stove coal Pintsch process gas
4Deng organism and unreacted and the reaction remaining fine breeze carry out the temperature raising twice transformation.Adjust gas composition and load, reduce CH in the reactant gases
4(less than 1.5%) and CO
2(less than 20%) content, the control dust is taken (reducing by 30%～50%) out of.
The 3rd feature of aforesaid method and equipment is: the top radiant coolers, adopted special structure formation (accompanying drawing 2a), and solved the heavy wear of the useless pot of general fluidized-bed radiation and the problem such as with high investment of back segment vapor superheater has been set.
The feature of aforesaid method and equipment also is: tornado dust collector, adopt circle or Sui circular gas inlet structure; Upper cover adopts the sphere or the butterfly end enclosure structure of liner ceiling.Under the prerequisite that satisfies the construction of pressure vessel requirement, can guarantee high efficiency of dust collection.Heat recovery equipment adopts water pipe cage construction and the combination order tubular construction of going up next part case, standpipe connection, transversal flow, owing to compact construction, efficient height, investment is descended; And satisfy requirement wear-resistant and that anti-caking is grey.
High temperature service and pipeline adopt liner corundum layer and heat insulation double-deck hot-wall structure of polycrystalline fibre plate and the cold wall containment structure of water jacket.Guaranteeing under the device security reliable conditions, not only improving device thermo-efficiency but also satisfied the heat resistanceheat resistant requirement of shaking.
Description of drawings
Fig. 1 is an apparatus structure schematic flow sheet of the present utility model
Fig. 2 is the structural representation of the utility model reactor
Fig. 3 is the emulsion zone conversion zone selectivity ash discharge structural representation of the utility model reactor
Fig. 4 is the cold and hot wall composite structure synoptic diagram of the utility model reactor
Fig. 5 is that the secondary reaction of the utility model reactor is adjusted section gasification agent inlet structural representation
Wherein:1:coal bunker 2:coal lock 3:feeding-coal bucket 4:star-like material feeder 5; 6： 7： 8： 9： 10： 11： 12： 3： 14： 15： 16： 17： 18： 19： 20： 21： 22： 23：24： 25： 26： 27：28： 29： 30： 31： 32： 33： 34： 35： 36： 37： 38： 39： 40： 41： 42： 43： 44：45： 46： 47： 48： 49： 50： 51： 52： 53： 54：55： 56： 57： 58： 59： 60： 61： 62： 63： 64：
Embodiment
Reaching embodiment in conjunction with the accompanying drawings can be further detailed the utility model
Embodiment 1
Specific implementation method shown in Figure 1 and equipment: feed coal is by the coal bunker (1) of coal system, coal lock (2) and feeding-coal bucket (3), enter reactor by coal inlet (41) on vaporized chemical sparger fluidising chamber (B) top of emulsion zone conversion zone (I), sparger nozzle vaporized chemical (17), sparger core jet pipe vaporized chemical (18), sparger endless tube vaporized chemical (19) and secondary air vaporized chemical (21) are respectively by sparger nozzle gasification agent inlet (45), select sparger endless tube gasification agent inlet (47), sparger core jet pipe gasification agent inlet (46) and secondary air inlet (44) enter reactor, and feed coal and vaporized chemical experience two sections close phase reaction sections of double fire layer (I) and secondary reaction in reactor, derive by top-side gas exit (43) after adjusting section (III) reaction and radiant cooler (5A).The reunion lime-ash (25) that forms in the reactor is discharged by selectivity ash discharge chamber (A) and behind cold slag machine (11), receipts slag bucket (12) and slag lock (13).The dust-laden coal gas that reactor head derives at first enters waste heat boiler (7) after high-temperature cyclone dust extractor (6) dedusting and oiler feed preheating (8), dry type porcelain filter (9) and washing tower (10) are sent system, the dust of high-temperature cyclone dust extractor (6) is further reacted by reactor returning charge mouth (42) Returning reactor, the ash (26) of dry type pottery fly-ash separator (9) through ash cooler (14), receive grey machine (15) and the discharge of ash lock (16) back.
The structure of concrete enforcement reactor shown in Figure 2, this reactor adopt the following greatly little concentric tube body structure of close phase reaction section (I) of last secondary reaction, adjustment section (III) with middle transition section (II).The ratio of its cross section should satisfy upward secondary reaction, close phase reaction section (I) the cross section gas superficial velocity reduction by 1/2 down of adjustment section (III) cross section gas superficial velocity ratio; Middle transition section (II) angle of rest (repose) should be less than 30 degree (with the vertical direction angle); Last secondary reaction, adjustment section (III) close phase reaction section (I) cylindrical shell height down should satisfy the throughput of reactor and the requirement of gas entrainment transport disengaging height (TDH); Last secondary reaction, adjustment section (III) cylindrical shell top are by sphere or butterfly end socket sealing (IV); Last secondary reaction, adjustment section (III) cylindrical shell upper side are provided with gas exit (43); Last secondary reaction, adjustment section (III) cylindrical shell gas exit (43) are provided with gas cooler (5A) down and apart from gas exit (43) minor increment; Bottom last secondary reaction, adjustment section (III) cylindrical shell and with the last tangent line minor increment of crossing middle transition section (II) secondary air inlet (44) is set; Down (I) cylindrical shell bottom is by vaporized chemical sparger (V) sealing of casting shape, in close phase reaction section (I) cylindrical shell bottom down and with the last tangent line minor increment of sparger (V) feed coal coal inlet (41) and returning charge mouth (42) is set and should as far as possible evenly arranges.This reactor has cold and hot wall compages, promptly adopt the cold wall containment structure of high temperature resistant, heat insulation double layer innerliner hot wall and water jacket, at least one chuck admission port (49) is set in the bottom of water jacket, on the reactor head end socket, arrange at least one chuck steam water interface outlet (52), and link to each other with upcast with the drum downtake that is installed at least 5 meters of reactor tops respectively, water jacket can produce normal pressure or middle pressure saturation steam according to different reactor operating pressures.
Gas distributor structure in the close phase reaction section of concrete enforcement reactor shown in Figure 3 (I), this gas distributor is made up of the positive casting body (B section) that is directly connected in close phase reaction section (I) cylindrical shell below (C section) and the straight tube (A section) of bottom minor diameter.About 45～60 degree of the angle of rest (repose) of positive casting body (B section) and at positive casting body (B section) circumference at least one ring is set, every ring is evenly equipped with three sparger nozzle gasification agent inlets (45) at least, the heap face of the vertical and positive casting body (B section) of sparger nozzle gasification agent inlet (45) angle, last ring spray mouth is apart from heap body upper hem section minimum, following ring spray mouth is apart from heap body lower hem section minimum, in the ring spray mouth arrange that between two parties nozzle quantity is with the vaporized chemical uniform distribution in the positive casting body (B section) be as the criterion (the nozzle number typical amount is 8,12 and 18); Positive casting body (B section) central section is provided with the spouted pipe of high speed of oxygen enrichment (oxygen concn 60%～85%), and (speed is about 20～40m/s), and draws by being positioned at heap body lower hem transition section bottom.The straight tube (A section) of bottom minor diameter, its internal diameter should satisfy the requirement (speed about 8～18m/s) of deslagging intensity and selective deslagging gas speed, about 800～the 1500mm of length, the side that straight tube (A section) slag-drip opening (48) is gone up about 200mm is provided with a sparger endless tube gasification agent inlet (47), and the slag of reuniting in the reactor is discharged by straight tube (A section) bottom.
Fig. 4 specifically implements the cold and hot wall composite structure of reactor synoptic diagram, and it includes the two kinds of structures in coil pipe in cooler position (a) and no coil pipe in cooler position (b).Two kinds of structures are formed, and are provided with numerous anchor nails (58) by inner core (62) and urceolus (61) and thermofin (57), refractory and antiwear layer (56) liner; The water jacket that all forms 50～100mm between inner core (62) and urceolus (61) is as cooling-water duct, and thermofin (57) all adopts calcium silicate board with microporous or the polycrystalline fibre plate of 30～50mm, and refractory and antiwear layer (56) all adopts diamond spar mould material or the diamond spar brick of 80～120mm.Two kinds of structure differences are that a part of shell ring of the inner core (62) in superheater coil (54) position (a) is replaced by superheater coil (54), and superheater coil (54) inboard is provided with different coil pipe anchor nails (59); The inboard thermofin (57) of superheater coil (54) is replaced by thermal conductivity and the better equal thickness silicon carbide layer of mechanicalness (55).In addition, the connection between superheater coil (54) is checked sheet (64) structure shown in (c), checks and carries out inside and outside hermetically sealed weldering between sheet (64) and superheater coil (54), and its welding zone (63) area should be greater than the heating surface of checking sheet (64).
Fig. 5 specifically implements the reactor secondary reaction to adjust the structural representation of section gasification agent inlet, go up (III) cylindrical shell bottom and with secondary air that the last tangent line minor increment of transition section (II) is provided with (44) its minimum number that enters the mouth be three; Can reach 15%～35% of total gasification dosage; Adding the inlet diameter is controlled at gas speed and is about 80～120m/s; Mounting arrangements is a circumference uniform distribution, and positive pitch is about 9～15 degree (with the horizontal direction angle), and clockwise about 7～18 degree in drift angle radially are so that air-flow rotation and be tangential on the secondary air inscribed circle (60) that virtual diameter is about 500～800mm.
The utility model is used for the method for fluid bed powder coal gasification reactor, the feed coal of this method is by coal bunker 1, coal lock 2 and the feeding-coal bucket 3 of coal system, enter reactor by coal inlet 41 on vaporized chemical sparger fluidising chamber (B) top of close phase reaction section (I), sparger nozzle vaporized chemical 17, sparger core jet pipe vaporized chemical 18, sparger endless tube vaporized chemical 19 and chuck import feedwater 21 enter reactor by sparger nozzle gasification agent inlet 45, selection sparger endless tube gasification agent inlet 47, sparger core jet pipe gasification agent inlet 46 and secondary air inlet 44 respectively; Feed coal and vaporized chemical experience two sections double fire layers (I, III) reaction in reactor and cooling (5A) back is derived by the gas exit 43 of top-side, and the reunion lime-ash 25 that forms in the reactor is discharged by selectivity ash discharge chamber (A) and behind cold slag machine 11, receipts slag bucket 12 and slag lock 13; The dust-laden coal gas that reactor head derives at first enters waste heat boiler 7, back boiler feed water preheater 8, dry type pottery fly-ash separator 9 and washing tower 10 and sends system after high-temperature cyclone dust extractor 6 dedustings, the dust of high-temperature cyclone dust extractor 6 is further reacted by reactor returning charge mouth 42 Returning reactors, and the fine dust ash 26 of dry type pottery fly-ash separator 9 is discharged behind ash cooler 14, receipts ash bucket 15 and ash trivial 16.
Claims (9)
1. fluid bed powder coal gasification reactor, it contains spouted fluidized close phase reaction section (I), secondary reaction, adjusts section (III) and a middle transition section (II); Close phase reaction section (I) and secondary reaction, adjustment section (III) are separately positioned on the below and the top of middle transition section (II), it is characterized in that close phase reaction section (I) below is communicated with the vaporized chemical sparger (V) of back taper; Secondary reaction, adjustment section (III) top are connected with radiant cooler (5A) and end socket (IV); (I, II, III, IV, V) adopts cold and hot wall compages on the reactor monolith.
2. fluid bed powder coal gasification reactor as claimed in claim 1, it is characterized in that close phase reaction section (I), secondary reaction, adjustment section (III) and middle transition section (II) are that going up of middle transition section (II) adjusted section (III) greatly, the following little concentric tube body structure of close phase reaction section (I), the ratio of its cross section are upward to adjust close phase reaction section (I) cross section gas superficial velocity reduction by 1/2 under the gas superficial velocity ratio of section (III) cross section; Middle transition section (II) cone angle and vertical direction angle are less than 30 degree; Last adjustment section (III), following close phase reaction section (I) cylindrical shell height satisfy the throughput and the isolating height of gas entrainment of reactor.
3. fluid bed powder coal gasification reactor as claimed in claim 1 is characterized in that secondary reaction, adjusts the cylindrical shell top of section (III) by sphere or butterfly end socket sealing (IV); Last adjustment section (III) cylindrical shell upper side is provided with gas exit (43) apart from sphere or butterfly end socket (IV) tangent distance; Distance apart from gas exit (43) under last adjustment section (III) cylindrical shell gas exit (43) is provided with gas cooler (5A); The last last tangent distance of adjusting section (III) cylindrical shell bottom and transition section (II) is provided with secondary air inlet (44).
4. fluid bed powder coal gasification reactor as claimed in claim 3 is characterized in that the quantity of secondary air inlet (44) is at least three, can reach 15%～35% of total gasification dosage; The gas speed that adds inlet is about 80～120m/s; Mounting arrangements is a circumference uniform distribution, and upwards and the horizontal direction angle be 9～15 degree, about 7～18 degree in drift angle clockwise radially are so that air-flow rotation and be tangential on the secondary air inscribed circle (60) that diameter is 500～800mm.
5. fluid bed powder coal gasification reactor as claimed in claim 1, it is characterized in that of vaporized chemical sparger (V) sealing of the cylindrical shell bottom of close phase reaction section (I) by back taper, be provided with coal inlet (41) and returning charge mouth (42) in following close phase reaction section (I) cylindrical shell bottom and with the last tangent line minor increment of sparger (V), itself and body of heater angle are 45～30 degree, and evenly arrange.
6. fluid bed powder coal gasification reactor as claimed in claim 1 is characterized in that gas distributor (V) directly is communicated with at the positive reverse taper of emulsion zone conversion zone (I) cylindrical shell below and the straight tube composition of base diameter in the close phase reaction section (I); About 45～60 degree of the cone angle of positive reverse taper and at positive reverse taper circumference at least one ring is set, every ring is evenly equipped with three sparger nozzle gasification agent inlets (45) at least; The conical surface of the vertical and positive reverse taper of sparger nozzle gasification agent inlet (45) angle, last ring spray mouth is apart from cone upper hem section, and following ring spray mouth is apart from cone lower hem section, and middle ring spray mouth is arranged between two parties, nozzle quantity is with the intravital vaporized chemical uniform distribution of positive back taper, and typical nozzle quantity is 8,12 and 18; The spouted pipe of high speed that positive reverse taper central section is provided with oxygen enrichment is positioned at cone lower hem transition section bottom; The bottom straight tube is arranged in the slag-drip opening (48) of reactor reunion slag, and side above it is provided with a sparger endless tube gasification agent inlet (47).
7. fluid bed powder coal gasification reactor as claimed in claim 1 is characterized in that reactor is the cold and hot wall composite structure that adopts double layer innerliner hot wall and the cold wall shell of water jacket.
8. fluid bed powder coal gasification reactor as claimed in claim 7, the bottom that it is characterized in that the cold wall shell of reactor water chuck is provided with at least one chuck admission port (49), at least one chuck steam water interface outlet (52) is set on the end socket of the top of reactor, and respectively be installed in reactor on the drum downtake be connected with upcast.
9. fluid bed powder coal gasification reactor as claimed in claim 7, it is characterized in that the coil pipe in cooler position (a) of reactor and no coil pipe in cooler position (b) constitute by inner core (62) and urceolus (61) and thermofin (57), refractory and antiwear layer (56) liner, and fixing by anchor nails (58); All form water jacket as cooling-water duct between inner core (62) and urceolus (61), thermofin (57) is calcium silicate board with microporous or polycrystalline fibre plate, and refractory and antiwear layer (56) is diamond spar mould material or diamond spar brick; Two kinds of structure differences are that a part of shell ring of the inner core (62) in superheater coil (54) position (a) is replaced by superheater coil (54), and the coil pipe in cooler inboard is provided with different coil pipe anchor nails (59); Inboard thermofin (57) and the silicon carbide layer (55) of superheater coil (54) replaced; Connection between superheater coil (54) is checked between sheet (64) and is tightly connected, and its joining region (63) area should be greater than the heating surface area of checking sheet (64).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620128241 CN201010630Y (en) | 2006-11-24 | 2006-11-24 | Fluid bed powder coal gasifying reactor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620128241 CN201010630Y (en) | 2006-11-24 | 2006-11-24 | Fluid bed powder coal gasifying reactor |
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| CN201010630Y true CN201010630Y (en) | 2008-01-23 |
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| CN 200620128241 Expired - Fee Related CN201010630Y (en) | 2006-11-24 | 2006-11-24 | Fluid bed powder coal gasifying reactor |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102071069A (en) * | 2010-11-25 | 2011-05-25 | 中国科学院山西煤炭化学研究所 | Device and method for regulating temperature of coal gas at outlet of fluidized bed gasifier |
| CN104981535A (en) * | 2012-12-12 | 2015-10-14 | 蒂森克虏伯工业解决方案股份公司 | Method for heating high temperature winkler gasifier |
| CN105524658A (en) * | 2016-01-10 | 2016-04-27 | 张勇 | Biomass fuel gas whole-process segmented purification method |
| CN107760385A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | Fluid bed and melting bed combined coal gasification apparatus and its method |
| CN110005846A (en) * | 2019-04-09 | 2019-07-12 | 北京石油化工工程有限公司 | Water sealed tank |
| CN112410076A (en) * | 2020-12-08 | 2021-02-26 | 中国科学院工程热物理研究所 | Air distribution slag cooling device and method for fluidized bed gasification furnace |
| CN115418235A (en) * | 2022-08-19 | 2022-12-02 | 合肥工业大学 | Multi-roller direct heat exchange type carbonization furnace |
-
2006
- 2006-11-24 CN CN 200620128241 patent/CN201010630Y/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102071069A (en) * | 2010-11-25 | 2011-05-25 | 中国科学院山西煤炭化学研究所 | Device and method for regulating temperature of coal gas at outlet of fluidized bed gasifier |
| CN104981535A (en) * | 2012-12-12 | 2015-10-14 | 蒂森克虏伯工业解决方案股份公司 | Method for heating high temperature winkler gasifier |
| CN105524658A (en) * | 2016-01-10 | 2016-04-27 | 张勇 | Biomass fuel gas whole-process segmented purification method |
| CN107760385A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | Fluid bed and melting bed combined coal gasification apparatus and its method |
| CN107760385B (en) * | 2016-08-23 | 2020-12-01 | 中国石油化工股份有限公司 | Coal gasification device combining fluidized bed and molten bed and method thereof |
| CN110005846A (en) * | 2019-04-09 | 2019-07-12 | 北京石油化工工程有限公司 | Water sealed tank |
| CN110005846B (en) * | 2019-04-09 | 2024-04-30 | 北京石油化工工程有限公司 | Water sealed tank |
| CN112410076A (en) * | 2020-12-08 | 2021-02-26 | 中国科学院工程热物理研究所 | Air distribution slag cooling device and method for fluidized bed gasification furnace |
| CN112410076B (en) * | 2020-12-08 | 2021-10-08 | 中国科学院工程热物理研究所 | Air distribution slag cooling device and method for fluidized bed gasification furnace |
| CN115418235A (en) * | 2022-08-19 | 2022-12-02 | 合肥工业大学 | Multi-roller direct heat exchange type carbonization furnace |
| CN115418235B (en) * | 2022-08-19 | 2023-08-25 | 合肥工业大学 | Multi-roller direct heat exchange type carbonization furnace |
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