CN104479704A - Oil shale semicoke fluidized combustion circulation gas heating technology - Google Patents
Oil shale semicoke fluidized combustion circulation gas heating technology Download PDFInfo
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- CN104479704A CN104479704A CN201410839156.9A CN201410839156A CN104479704A CN 104479704 A CN104479704 A CN 104479704A CN 201410839156 A CN201410839156 A CN 201410839156A CN 104479704 A CN104479704 A CN 104479704A
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- gas
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- heating
- heat exchanger
- interchanger
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/06—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of oil shale and/or or bituminous rocks
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
- C10B49/08—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
- C10B49/10—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form according to the "fluidised bed" technique
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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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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
- Dispersion Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
Abstract
An oil shale semicoke fluidized combustion and circulation gas heating technology is characterized by comprising the steps of sending oil shale semicoke greater than 0-15mm and residual gas into a fluid bed for low temperature combustion, heating circulation gas flowing in a diaphragm wall heat exchanger with a part of heat released by the combustion, discharging the other part of heat along with smoke generated by the combustion after exchanging heat with a tubular heat exchanger, allowing high-temperature ash and slag generated by the combustion of the semicoke to enter a fluid bed slag cooler for cooling, conveying cooled low-temperature ash and slag to a slag yard, allowing smoke to carry fly ash generated by the combustion to be discharged after exchanging the heat with a high-temperature air preheating tubular heat exchanger, a medium-high temperature gas heating tubular heat exchanger and a low-temperature air preheating tubular heat exchanger, mixing the circulation gas after heating cold circulation gas from a cold gas main line via the diaphragm wall heat exchanger with the cold gas, heating the mixed gas, and allowing the smoke temperature at an outlet of a hearth to be 850-950 DEG C, and hot circulation gas temperature at a hot gas outlet to be less than 720 DEG C.
Description
Technical field
The present invention relates to resinous shale gaseous heat-carrier retorting technique field.Be a kind of oil shale semi-coke fluidized bed combustion circulating mash gas heating technology, this technique 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.
The most widely used Fushun type retort of current domestic oil shale distillation, adopts recuperative heater.The working process of recuperative heater 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 coal mine 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.
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 producer 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 object of the invention is, substantial improvements is carried out to the existing operational path 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 heating technology, 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, there is comprehensive utilization degree high, the advantages such as cost is low, scientific and reasonable.
The object of the invention is to be realized by following technical scheme: a kind of oil shale semi-coke fluidized bed combustion circulating mash gas heating technology, it is characterized in that, it has in comprising: > 0 ~ 15mm oil shale semi-coke is sent into fluidized-bed burner hearth from opening for feed, tail gas sends into fluidized-bed burner hearth from tail gas burner, after semicoke and tail gas enter fluidized-bed burner hearth, low-temperature burning at 850 ~ 950 DEG C; The circulating mash gas that semicoke and tail gas flow in the heat part heating furnace surrounding membrane wall interchanger that fluid bed furnace chamber inner combustion discharges, a part flows through high temperature air preheating tubular heat exchanger, high temperature gas heating tube formula interchanger, middle Wen Wasi heating heated Tube interchanger and Cryogenic air preheating tubular heat exchanger successively with the flue gas that burning produces, be 120 ~ 200 DEG C with the flue-gas temperature after tubular heat exchanger heat exchange, discharge from exhanst gas outlet; The high-temperature ash that coal-char combustion produces enters fluidized bed slag cooler from deslagging overflow port, high-temperature ash becomes low temperature lime-ash after cooling, can directly be transported to slag field, the flying dust that burning produces is carried by flue gas, flow through high temperature air preheating tubular heat exchanger, high temperature gas heating tube formula interchanger, middle Wen Wasi heating heated Tube interchanger and Cryogenic air preheating tubular heat exchanger successively, the temperature of final 120 ~ 200 DEG C is discharged from exhanst gas outlet; The cold First air come from primary air fan is heated as heat primary air feeding burner hearth through Cryogenic air preheating tubular heat exchanger and high temperature air preheating tubular heat exchanger successively, heat primary air temperature is 350 ~ 450 DEG C, higher than the kindling temperature of oil shale semi-coke, be conducive to catching fire and stable burning of semicoke, the cold secondary air come from overfire air fan becomes hot secondary air after cooling down high-temperature lime-ash in fluidized bed slag cooler, overfire air port in the middle part of burner hearth is sent into, oxygen needed for the aftercombustion later stage, takes full advantage of again the physical sensible heat of lime-ash; The SAPMAC method gas come from cold gas Trunk Line evenly enters membrane wall interchanger by influent header, the SAPMAC method gas come from cold gas Trunk Line enters mixing header by variable valve, after the heating of membrane wall interchanger, the circulating mash gas of 150 ~ 300 DEG C enters the middle Wen Wasi heating heated Tube interchanger of afterbody, circulating mash gas is heated to 450 ~ 550 DEG C in middle Wen Wasi heating heated Tube interchanger, enter mixing header subsequently, mix with regulating the cold gas of temperature in mixing header, mixed circulating mash gas enters high temperature gas heating tube formula interchanger; Circulating mash gas is heated to 600 ~ 720 DEG C in high temperature gas heating tube formula interchanger, enter hot gas export header, by regulating the consumption of primary and secondary air and semicoke, tail gas, the cigarette temperature at furnace outlet place is made to be 850 ~ 950 DEG C, the cold gas flow entering mixing header is regulated by variable valve, make the thermal circulation gas temperature < 720 DEG C of hot gas export header, thus avoid the cracking carbon distribution of circulating mash gas.
The advantage applies of oil shale semi-coke fluidized bed combustion circulating mash gas heating technology of the present invention exists:
1. heat required during oil shale distillation comes from semicoke circulating fluidized bed combustion, utilizes oil shale semi-coke, realizes energy-autarchic to all shale;
2. the flue-gas temperature that hearth combustion produces is stable, and the cigarette temperature at furnace outlet place is at 850 ~ 950 DEG C, and circulating mash gas can remain on < 720 DEG C, is conducive to the normal table running of gas retort;
3. 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;
4. flying dust and ash content carbon are lower than 2%, therefore without the need to carrying out roasting again, can deliver to cement building material factory cement, Building Materials Factory's potting grain and/or building block by direct effect raw material of building materials;
5. burning First air is preheated to 350 ~ 450 DEG C and sends into burner hearth, higher than the kindling temperature of oil shale semi-coke, is conducive to catching fire and stable burning of semicoke;
6. there is mixing header between high temperature gas heating zone and middle Wen Wasi heating zone, by regulating the cold gas flow entering mixing header, making thermal circulation gas temperature < 720 DEG C, thus avoiding the cracking carbon distribution of circulating mash gas;
7. secondary air becomes warm air after cooling down high-temperature lime-ash in fluidized bed slag cooler, sends in the middle part of burner hearth, and oxygen needed for the aftercombustion later stage takes full advantage of again the physical sensible heat of lime-ash.
Accompanying drawing explanation
Fig. 1 is oil shale semi-coke fluidized bed combustion circulating mash gas heating technology schema.
In figure: 1 fluidized-bed burner hearth, 2 membrane wall interchanger, 3 opening for feeds, 4 tail gas burners, 5 overfire air ports, 6 cold gas inlet headers, 7 cold gas Trunk Lines, 8 deslagging overflow ports, 9 fluidized bed slag coolers, 10 overfire air fans, 11 primary air fans, 12 exhanst gas outlets, 13 Cryogenic air preheating tubular heat exchangers, warm gas heating tube formula interchanger in 14,15 variable valve, 16 hot gas export headers, 17 high temperature gas heating tube formula interchanger, 18 mixing headers, 19 high temperature air preheating tubular heat exchangers.
Embodiment
The invention will be further described to utilize drawings and Examples below.
With reference to Fig. 1, oil shale semi-coke fluidized bed combustion circulating mash gas heating technology of the present invention, > 0 ~ 15mm oil shale semi-coke is sent into fluidized-bed burner hearth 1 from opening for feed 3, tail gas sends into fluidized-bed burner hearth 1 from tail gas burner 4, and semicoke and tail gas to enter after fluidized-bed burner hearth 1 low-temperature burning at 850 ~ 950 DEG C; The circulating mash gas of semicoke and tail gas flowing in the heat part heating furnace surrounding membrane wall interchanger 2 that fluidized-bed burner hearth 1 combustion discharges, a part flows through high temperature air preheating tubular heat exchanger 19, high temperature gas heating tube formula interchanger 17, middle Wen Wasi heating heated Tube interchanger 14 and Cryogenic air preheating tubular heat exchanger 13 successively with the flue gas that burning produces, be 120 ~ 200 DEG C with the flue-gas temperature after tubular heat exchanger heat exchange, discharge from exhanst gas outlet 12.The high-temperature ash that coal-char combustion produces enters fluidized bed slag cooler 9 from deslagging overflow port 8, and high-temperature ash becomes low temperature lime-ash after cooling, can directly be transported to slag field.The flying dust that burning produces is carried by flue gas, flow through high temperature air preheating tubular heat exchanger 19, high temperature gas heating tube formula interchanger 17, middle Wen Wasi heating heated Tube interchanger 14 and Cryogenic air preheating tubular heat exchanger 13 successively, outlet temperature is 120 ~ 200 DEG C, discharges from exhanst gas outlet 12.Be heated as heat primary air through Cryogenic air preheating tubular heat exchanger 13 and high temperature air preheating tubular heat exchanger 19 successively from the cold First air of primary air fan 11 and send into burner hearth 1, heat primary air temperature is 350 ~ 450 DEG C, higher than the kindling temperature of oil shale semi-coke, be conducive to catching fire and stable burning of semicoke.In fluidized bed slag cooler 9, become hot secondary air from the cold secondary air of overfire air fan 10 after cooling down high-temperature lime-ash, the overfire air port 5 in the middle part of burner hearth 1 is sent into, and oxygen needed for the aftercombustion later stage takes full advantage of again the physical sensible heat of lime-ash.Membrane wall interchanger 2 is evenly entered by influent header 6 from the SAPMAC method gas of cold gas Trunk Line 7, mixing header 18 is entered by variable valve 15 from the SAPMAC method gas of cold gas Trunk Line 7, after membrane wall interchanger 2 heats, the circulating mash gas of 150 ~ 300 DEG C enters the middle Wen Wasi heating heated Tube interchanger 14 of afterbody, circulating mash gas is heated to 450 ~ 550 DEG C in middle Wen Wasi heating heated Tube interchanger 14, enter mixing header 18 subsequently, mix with regulating the cold gas of temperature in mixing header 18, mixed circulating mash gas enters high temperature gas heating tube formula interchanger 17.Circulating mash gas is heated to 600 ~ 720 DEG C in high temperature gas heating tube formula interchanger 17, enters hot gas export header 16, by regulating the consumption of primary and secondary air and semicoke, tail gas, makes the cigarette temperature at furnace outlet place be 850 ~ 950 DEG C.Regulated the cold gas flow entering mixing header 18 by variable valve 15, make the thermal circulation gas temperature < 720 DEG C of hot gas export header 16, thus avoid the cracking carbon distribution of circulating mash gas.
Oil shale semi-coke fluidized bed combustion circulating mash gas heating technology of the present invention is only specific embodiment, and non exhaustive, and those skilled in the art copy and improve the scope that should belong to the claims in the present invention and protect without creative work.
Claims (1)
1. an oil shale semi-coke fluidized bed combustion circulating mash gas heating technology, it is characterized in that, it has in comprising: > 0 ~ 15mm oil shale semi-coke is sent into fluidized-bed burner hearth from opening for feed, tail gas sends into fluidized-bed burner hearth from tail gas burner, after semicoke and tail gas enter fluidized-bed burner hearth, low-temperature burning at 850 ~ 950 DEG C; The circulating mash gas that semicoke and tail gas flow in the heat part heating furnace surrounding membrane wall interchanger that fluid bed furnace chamber inner combustion discharges, a part flows through high temperature air preheating tubular heat exchanger, high temperature gas heating tube formula interchanger, middle Wen Wasi heating heated Tube interchanger and Cryogenic air preheating tubular heat exchanger successively with the flue gas that burning produces, be 120 ~ 200 DEG C with the flue-gas temperature after tubular heat exchanger heat exchange, discharge from exhanst gas outlet; The high-temperature ash that coal-char combustion produces enters fluidized bed slag cooler from deslagging overflow port, high-temperature ash becomes low temperature lime-ash after cooling, can directly be transported to slag field, the flying dust that burning produces is carried by flue gas, flow through high temperature air preheating tubular heat exchanger, high temperature gas heating tube formula interchanger, middle Wen Wasi heating heated Tube interchanger and Cryogenic air preheating tubular heat exchanger successively, the temperature of final 120 ~ 200 DEG C is discharged from exhanst gas outlet; The cold First air come from primary air fan is heated as heat primary air feeding burner hearth through Cryogenic air preheating tubular heat exchanger and high temperature air preheating tubular heat exchanger successively, heat primary air temperature is 350 ~ 450 DEG C, higher than the kindling temperature of oil shale semi-coke, be conducive to catching fire and stable burning of semicoke, the cold secondary air come from overfire air fan becomes hot secondary air after cooling down high-temperature lime-ash in fluidized bed slag cooler, overfire air port in the middle part of burner hearth is sent into, oxygen needed for the aftercombustion later stage, takes full advantage of again the physical sensible heat of lime-ash; The SAPMAC method gas come from cold gas Trunk Line evenly enters membrane wall interchanger by influent header, the SAPMAC method gas come from cold gas Trunk Line enters mixing header by variable valve, after the heating of membrane wall interchanger, the circulating mash gas of 150 ~ 300 DEG C enters the middle Wen Wasi heating heated Tube interchanger of afterbody, circulating mash gas is heated to 450 ~ 550 DEG C in middle Wen Wasi heating heated Tube interchanger, enter mixing header subsequently, mix with regulating the cold gas of temperature in mixing header, mixed circulating mash gas enters high temperature gas heating tube formula interchanger; Circulating mash gas is heated to 600 ~ 720 DEG C in high temperature gas heating tube formula interchanger, enter hot gas export header, by regulating the consumption of primary and secondary air and semicoke, tail gas, the cigarette temperature at furnace outlet place is made to be 850 ~ 950 DEG C, the cold gas flow entering mixing header is regulated by variable valve, make the thermal circulation gas temperature < 720 DEG C of hot gas export header, thus avoid the cracking carbon distribution of circulating mash gas.
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| CN201410839156.9A CN104479704B (en) | 2014-12-30 | 2014-12-30 | Oil shale semicoke fluidized combustion circulation gas heating technology |
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| CN201410839156.9A CN104479704B (en) | 2014-12-30 | 2014-12-30 | Oil shale semicoke fluidized combustion circulation gas heating technology |
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| CN104479704B CN104479704B (en) | 2017-02-22 |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4700639A (en) * | 1983-03-16 | 1987-10-20 | Gerald Esterson | Utilization of low grade fuels |
| CN101362954A (en) * | 2008-09-26 | 2009-02-11 | 沈阳成大弘晟能源研究院有限公司 | Semi-coke gas multifuel combustion furnace |
| CN101818073A (en) * | 2010-05-21 | 2010-09-01 | 上海交通大学 | Dry distillation and semicoke incineration integrated system for oil shale |
| CN102295941A (en) * | 2011-07-29 | 2011-12-28 | 上海交通大学 | Combined system of oil shale bubble column dry distillation and semicoke circulating fluidized bed combustion |
| CN102952558A (en) * | 2012-11-16 | 2013-03-06 | 东北电力大学 | Integral process for oil shale drying, heating, refining and semicoke burning |
| CN103604121A (en) * | 2013-11-29 | 2014-02-26 | 重庆大学 | Oil shale semicoke fluidized bed combustion system adopting triple-channel shunting control refeeder |
-
2014
- 2014-12-30 CN CN201410839156.9A patent/CN104479704B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4700639A (en) * | 1983-03-16 | 1987-10-20 | Gerald Esterson | Utilization of low grade fuels |
| CN101362954A (en) * | 2008-09-26 | 2009-02-11 | 沈阳成大弘晟能源研究院有限公司 | Semi-coke gas multifuel combustion furnace |
| CN101818073A (en) * | 2010-05-21 | 2010-09-01 | 上海交通大学 | Dry distillation and semicoke incineration integrated system for oil shale |
| CN102295941A (en) * | 2011-07-29 | 2011-12-28 | 上海交通大学 | Combined system of oil shale bubble column dry distillation and semicoke circulating fluidized bed combustion |
| CN102952558A (en) * | 2012-11-16 | 2013-03-06 | 东北电力大学 | Integral process for oil shale drying, heating, refining and semicoke burning |
| CN103604121A (en) * | 2013-11-29 | 2014-02-26 | 重庆大学 | Oil shale semicoke fluidized bed combustion system adopting triple-channel shunting control refeeder |
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| CN104479704B (en) | 2017-02-22 |
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