CN204369809U - Oil shale semi-coke fluidized bed combustion circulating mash gas process furnace - Google Patents
Oil shale semi-coke fluidized bed combustion circulating mash gas process furnace Download PDFInfo
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- CN204369809U CN204369809U CN201420858672.1U CN201420858672U CN204369809U CN 204369809 U CN204369809 U CN 204369809U CN 201420858672 U CN201420858672 U CN 201420858672U CN 204369809 U CN204369809 U CN 204369809U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
A kind of oil shale semi-coke fluidized bed combustion circulating mash gas process furnace, be characterized in, comprise the furnace outlet of fluid-bed combustion furnace and the inlet communication of afterbody tubular heat exchanger, the lower end of fluid-bed combustion furnace burner hearth connects air-distributing device, burner hearth front wall is provided with feed-pipe, rear wall is provided with deslagging upflow tube, the bottom of burner hearth is provided with tail gas burner and overfire air port, the surrounding of burner hearth is equipped with the membrane wall interchanger of heating cold cycle gas, afterbody tubular heat exchanger comprises high temperature, middle Wen Wasi tubular heater and high temperature, Cryogenic air preheating tubular heat exchanger, cold gas Trunk Line respectively with the influent header of the membrane wall interchanger of fluid-bed combustion furnace, the mixing header of afterbody tubular heat exchanger connects, the outlet header of the membrane wall interchanger of fluid-bed combustion furnace is connected with the middle temperature gas inlet of afterbody tubular heat exchanger, the hot air outlet of afterbody tubular heat exchanger respectively with the First air entrance of the air-distributing device of fluid-bed combustion furnace, the overfire air port of fluid-bed combustion furnace connects.
Description
Technical field
The utility model relates to the device heated circulating mash gas in resinous shale gaseous heat-carrier distillation process.This device also can be used for coal, junked tire, plastics, biomass.
Background technology
Resinous shale is a kind of important Energy resources, and world's oil shale resources standing stock are very huge, and its reserves are up to (10 ~ 15) × 10
18kJ, accounts for global various energy total amount (26 ~ 43) × 10
1835% of kJ, higher than world's crude oil known reserves (8 × 10
18~ 10 × 10
18kJ).
The exploitation of resinous shale mainly adopt the operational path based on gas retort to carry out destructive distillation oil refining at present, the existing operational path based on gas retort is based on gaseous heat-carrier: utilize thermal circulation gas to add in the middle part of gas retort as main heating carrier and heat retorted shale, and thermal circulation gas is heated by the process furnace independently arranged.
Existing recuperative heater working process is interval, first burn in stove inner combustion chamber with cold coal mine gas and air, heat smoke passes through regenerator, after filler checker brick heating certain hour, namely cut off burning coal mine gas and air, then pass into SAPMAC method coal mine gas, SAPMAC method gas obtains heat from filler checker brick, become thermal circulation gas gas, enter gas retort and heat dry rectificating oil shale as gaseous heat-carrier.After the filler checker brick of recuperative heater are cooled gradually, then pass into circulation gas and air, rekindle to heat filler.Circulating-heating like this, heat exchange.
Because recuperative heater is discontinuous, the thermal circulation gas temperature degree entering gas retort is changed within the scope of 550 ~ 750 DEG C, cause temperature cycle change in gas retort thus, cause whole device operate unstable and affect oily yield.
Existing tubular oven can stably operate continuously, makes the temperature of thermal circulation gas more constant, is conducive to the normal operation of gas retort.The thermal source of the tubular oven used in domestic and international gaseous heat-carrier retorting technique is main all from the tail gas that oil shale distillation produces, but for the resinous shale in most of mining area, tail gas burns the shortage of heat that can send to provide oil shale distillation institute heat requirement, needs separately to establish producer gas generator to produce the supplemental heat source of coal gas as hotblast stove.
Produce a large amount of semicokes after gaseous heat-carrier destructive distillation, not yet reasonably utilized at present.These semicoke calorific values are low, and containing more pollutent, heap is abandoned and occupied a large amount of soil, both wastes the energy, and causes serious pollution again to environment.
Summary of the invention
The purpose of this utility model is, substantial improvements is carried out to the existing process furnace with coal mine gas combustion heating circulating mash gas, membrane wall interchanger, afterbody tubular heat exchanger in oil shale semi-coke fluidized-bed combustion and stove are organically integrated and form oil shale semi-coke fluidized bed combustion circulating mash gas process furnace, both oil shale distillation coal-char combustion problem had been efficiently solved, achieve again the heating problems of hot gas needed for gaseous heat-carrier, have rational in infrastructure, comprehensive utilization degree is high, low cost and other advantages.
The purpose of this utility model is realized by following technical scheme: a kind of oil shale semi-coke fluidized bed combustion circulating mash gas process furnace, it is characterized in that: oil shale semi-coke fluidized bed combustion circulating mash gas process furnace, it is characterized in that, it comprises: the furnace outlet of fluid-bed combustion furnace and the inlet communication of afterbody tubular heat exchanger, fluid-bed combustion furnace comprises burner hearth, air-distributing device, overfire air port, tail gas burner, feed-pipe and deslagging upflow tube, the lower end of burner hearth connects air-distributing device, burner hearth front wall is provided with feed-pipe, rear wall is provided with deslagging upflow tube, the top of burner hearth is freeboard of fluidized bed, bottom is emulsion zone, tail gas burner and overfire air port is provided with bottom freeboard of fluidized bed, freeboard of fluidized bed surrounding is furnished with the membrane wall interchanger of heating cold cycle gas, the furnace wall that refractory materials forms burner hearth perisporium is laid inside membrane wall interchanger, the upper end of membrane wall interchanger is provided with outlet header, the lower end of membrane wall interchanger is provided with influent header, the sidewall of air-distributing device is provided with First air entrance, afterbody tubular heat exchanger is included in back-end ductwork and sets gradually high temperature air preheating tubular heat exchanger from top to bottom, high temperature gas tubular heater, middle Wen Wasi tubular heater and Cryogenic air preheating tubular heat exchanger, the back-end ductwork of Cryogenic air preheating tubular heat exchanger position is provided with cool air inlet, the sidewall of back-end ductwork lower end is provided with exhanst gas outlet, warm gas inlet during the back-end ductwork of middle Wen Wasi tubular heater position is provided with, back-end ductwork between high temperature gas tubular heater and middle Wen Wasi tubular heater is provided with mixing header, the back-end ductwork sidewall of high temperature gas tubular heater position is provided with hot gas export header, the back-end ductwork sidewall of high temperature air preheating tubular heat exchanger position is provided with hot air outlet, cold gas Trunk Line is connected with the influent header of the membrane wall interchanger of fluid-bed combustion furnace, cold gas Trunk Line is connected by the mixing header of variable valve with afterbody tubular heat exchanger, the outlet header of the membrane wall interchanger of fluid-bed combustion furnace is connected with the middle temperature gas inlet of afterbody tubular heat exchanger, and the hot air outlet of afterbody tubular heat exchanger is connected with the First air entrance of the air-distributing device of fluid-bed combustion furnace, the overfire air port of fluid-bed combustion furnace respectively.
The advantage applies of the utility model oil shale semi-coke fluidized bed combustion circulating mash gas process furnace exists:
1. heat required during oil shale distillation mainly comes from semicoke fluidized-bed combustion, utilizes oil shale semi-coke, realizes energy-autarchic to all shale;
2. the furnace wall that refractory materials forms burner hearth perisporium is laid in the inner side of membrane wall interchanger 2, namely alleviates furnace wall weight, reduces burner hearth and leaks out, heated again circulating mash gas gas, avoids simultaneously and to leak gas the danger caused to the wearing and tearing of film heat surface;
3. the flue-gas temperature after high temperature air preheating tubular heat exchanger is down to 750 ~ 850 DEG C, thus protection high temperature gas tubular type heater tube wall can not overtemperature;
4. circulating mash gas flows in tubular heat exchanger, can not be mixed into flue gas;
5. the semicoke of discharging with gas retort is for main fuel, and remaining coal mine gas is auxiliary fuel, adopts fluidized-bed or circulating fluidized bed combustion mode, effectively utilizes low heat value semicoke, solves semicoke simultaneously and stacks the environmental issue caused;
6. high temperature gas tubular heater, down current arrangement, its material is silicon carbide, can suppress circulating mash gas cracking carbon distribution at high temperature;
7. there is mixing header between high temperature gas tubular heater and middle Wen Wasi tubular heater, by regulating the cold gas flow entering mixing header, making thermal circulation gas temperature not higher than 720 DEG C, thus avoiding the cracking carbon distribution of circulating mash gas;
8. it is rational in infrastructure, long service life, and resinous shale comprehensive utilization degree is high, and cost is low.
Accompanying drawing explanation
Fig. 1 is oil shale semi-coke fluidized bed combustion circulating mash gas process furnace figure.
In figure: 1 burner hearth, 2 membrane wall interchanger, 3 feed-pipes, 4 tail gas burners, 5 overfire air ports, 6 cold gas inlet headers, 7 cold gas Trunk Lines, 8 deslagging upflow tubes, 9 air-distributing devices, 10 First air entrances, 11 cool air inlets, 12 exhanst gas outlets, 13 Cryogenic air preheating tubular heat exchangers, Wen Wasi tubular heater in 14, 15 variable valve, 16 hot gas export headers, 17 high temperature gas tubular heaters, 18 mixing headers, 19 high temperature air preheating tubular heat exchangers, 20 membrane wall heat exchanger exit headers, 21 back-end ductworks, 22 furnace outlets, 23 afterbody tubular heat exchangers, 24 fluid-bed combustion furnaces, 25 freeboard of fluidized bed, 26 emulsion zones, 27 hot air outlets, warm gas inlet in 28.
Embodiment
The utility model is described in further detail to utilize drawings and Examples below.
Oil shale semi-coke fluidized bed combustion circulating mash gas process furnace of the present utility model, comprise the furnace outlet 22 of fluid-bed combustion furnace 24 and the inlet communication of afterbody tubular heat exchanger 23, fluid-bed combustion furnace 24 comprises burner hearth 1, air-distributing device 9, overfire air port 5, tail gas burner 4, feed-pipe 3 and deslagging upflow tube 8, the lower end of burner hearth 1 connects air-distributing device 9, burner hearth 1 front wall is provided with feed-pipe 3, rear wall is provided with deslagging upflow tube 8, the top of burner hearth 1 is freeboard of fluidized bed 25, bottom is emulsion zone 26, tail gas burner 4 and overfire air port 5 is provided with bottom freeboard of fluidized bed 25, freeboard of fluidized bed 25 surrounding is furnished with the membrane wall interchanger 2 of heating cold cycle gas, the furnace wall that refractory materials forms burner hearth perisporium is laid inside membrane wall interchanger, the upper end of membrane wall interchanger 2 is provided with outlet header 20, the lower end of membrane wall interchanger 2 is provided with influent header 6, the sidewall of air-distributing device 9 is provided with First air entrance 10, afterbody tubular heat exchanger 23 is included in back-end ductwork 21 and sets gradually high temperature air preheating tubular heat exchanger 19 from top to bottom, high temperature gas tubular heater 17, middle Wen Wasi tubular heater 14 and Cryogenic air preheating tubular heat exchanger 13, the back-end ductwork 21 of Cryogenic air preheating tubular heat exchanger 13 position is provided with cool air inlet 11, the sidewall of back-end ductwork 21 lower end is provided with exhanst gas outlet 12, warm gas inlet 28 during the back-end ductwork 21 of middle Wen Wasi tubular heater 14 position is provided with, back-end ductwork 21 between high temperature gas tubular heater 17 and middle Wen Wasi tubular heater 14 is provided with mixing header 18, back-end ductwork 21 sidewall of high temperature gas tubular heater 17 position is provided with hot gas export header 16, back-end ductwork 21 sidewall of high temperature air preheating tubular heat exchanger 19 position is provided with hot air outlet 27, cold gas Trunk Line 7 is connected with the influent header 6 of the membrane wall interchanger 2 of fluid-bed combustion furnace 24, cold gas Trunk Line 7 is connected with the mixing header 18 of afterbody tubular heat exchanger 23 by variable valve 15, the outlet header 20 of the membrane wall interchanger 2 of fluid-bed combustion furnace 24 is connected with the middle temperature gas inlet 28 of afterbody tubular heat exchanger 23, and the hot air outlet 27 of afterbody tubular heat exchanger 23 is connected with the First air entrance 10 of the air-distributing device 9 of fluid-bed combustion furnace 24, the overfire air port 5 of fluid-bed combustion furnace 24 respectively.
Oil shale semi-coke fluidized bed combustion circulating mash gas process furnace of the present utility model, sends the oil shale semi-coke of 0 ~ 15mm and tail gas into fluid-bed combustion furnace 24, after semicoke and tail gas enter burner hearth 1, and low-temperature burning at 850 ~ 950 DEG C; Circulating mash gas in the heat part heating furnace 1 surrounding membrane wall interchanger 2 of burning release, the heat smoke that a part produces with burning enters afterbody tubular heat exchanger 23 heating cycle gas and air.
Oil shale semi-coke fluidized bed combustion circulating mash gas process furnace of the present utility model is only specific embodiment, and non exhaustive, and those skilled in the art copy and improve the scope that should belong to the utility model claim and protect without creative work.
Claims (1)
1. an oil shale semi-coke fluidized bed combustion circulating mash gas process furnace, it is characterized in that: it comprises the furnace outlet of fluid-bed combustion furnace and the inlet communication of afterbody tubular heat exchanger, fluid-bed combustion furnace comprises burner hearth, air-distributing device, overfire air port, tail gas burner, feed-pipe and deslagging upflow tube, the lower end of burner hearth connects air-distributing device, burner hearth front wall is provided with feed-pipe, rear wall is provided with deslagging upflow tube, the top of burner hearth is freeboard of fluidized bed, bottom is emulsion zone, tail gas burner and overfire air port is provided with bottom freeboard of fluidized bed, freeboard of fluidized bed surrounding is furnished with the membrane wall interchanger of heating cold cycle gas, the furnace wall that refractory materials forms burner hearth perisporium is laid inside membrane wall interchanger, the upper end of membrane wall interchanger is provided with outlet header, the lower end of membrane wall interchanger is provided with influent header, the sidewall of air-distributing device is provided with First air entrance, afterbody tubular heat exchanger is included in back-end ductwork and sets gradually high temperature air preheating tubular heat exchanger from top to bottom, high temperature gas tubular heater, middle Wen Wasi tubular heater and Cryogenic air preheating tubular heat exchanger, the back-end ductwork of Cryogenic air preheating tubular heat exchanger position is provided with cool air inlet, the sidewall of back-end ductwork lower end is provided with exhanst gas outlet, warm gas inlet during the back-end ductwork of middle Wen Wasi tubular heater position is provided with, back-end ductwork between high temperature gas tubular heater and middle Wen Wasi tubular heater is provided with mixing header, the back-end ductwork sidewall of high temperature gas tubular heater position is provided with hot gas export header, the back-end ductwork sidewall of high temperature air preheating tubular heat exchanger position is provided with hot air outlet, cold gas Trunk Line is connected with the influent header of the membrane wall interchanger of fluid-bed combustion furnace, cold gas Trunk Line is connected by the mixing header of variable valve with afterbody tubular heat exchanger, the outlet header of the membrane wall interchanger of fluid-bed combustion furnace is connected with the middle temperature gas inlet of afterbody tubular heat exchanger, and the hot air outlet of afterbody tubular heat exchanger is connected with the First air entrance of the air-distributing device of fluid-bed combustion furnace, the overfire air port of fluid-bed combustion furnace respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420858672.1U CN204369809U (en) | 2014-12-30 | 2014-12-30 | Oil shale semi-coke fluidized bed combustion circulating mash gas process furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420858672.1U CN204369809U (en) | 2014-12-30 | 2014-12-30 | Oil shale semi-coke fluidized bed combustion circulating mash gas process furnace |
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|---|---|
| CN204369809U true CN204369809U (en) | 2015-06-03 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420858672.1U Expired - Fee Related CN204369809U (en) | 2014-12-30 | 2014-12-30 | Oil shale semi-coke fluidized bed combustion circulating mash gas process furnace |
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| CN (1) | CN204369809U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112393255A (en) * | 2019-08-16 | 2021-02-23 | 上海城投污水处理有限公司 | Combustor protection system for sludge co-combustion of sludge incinerator |
| CN112393253A (en) * | 2019-08-16 | 2021-02-23 | 上海城投污水处理有限公司 | Temperature rise control system for sludge incinerator and control method thereof |
-
2014
- 2014-12-30 CN CN201420858672.1U patent/CN204369809U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112393255A (en) * | 2019-08-16 | 2021-02-23 | 上海城投污水处理有限公司 | Combustor protection system for sludge co-combustion of sludge incinerator |
| CN112393253A (en) * | 2019-08-16 | 2021-02-23 | 上海城投污水处理有限公司 | Temperature rise control system for sludge incinerator and control method thereof |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150603 Termination date: 20161230 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |