CN104164257A - Fischer-Tropsch reactor pure-oxygen continuous gasification apparatus and gasification technology - Google Patents
Fischer-Tropsch reactor pure-oxygen continuous gasification apparatus and gasification technology Download PDFInfo
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- CN104164257A CN104164257A CN201410370202.5A CN201410370202A CN104164257A CN 104164257 A CN104164257 A CN 104164257A CN 201410370202 A CN201410370202 A CN 201410370202A CN 104164257 A CN104164257 A CN 104164257A
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Abstract
A Fischer-Tropsch reactor pure-oxygen continuous gasification apparatus comprises a coke-adding machine, a pure-oxygen gasification furnace, a cyclone separator, a sensible-heat recoverer, a gasifying agent preheater and a mixing tank; the height-diameter ratio of the pure-oxygen gasification furnace is 2.4-3.2; the mixing tank is provided with an oxygen inlet and a steam inlet, and is connected with the gasifying agent preheater via a pipe; the satisfying agent preheater is connected with the pure-oxygen gasifying furnace via a pipe; the top of the pure-oxygen satisfying furnace is connected with the coke-adding machine; the upper part of the pure-oxygen gasifying furnace is connected with the cyclone separator via a pipe; and the cyclone separator is connected with the sensible-heat recoverer. According to the apparatus and a gasification technology using the apparatus, the disadvantages of a conventional coal gasification technology are eliminated, no waste gas is discharged, and the effective gas content is high and is improved by 10% or more compared with that of other normal-pressure coal gasification technologies.
Description
Technical field
The present invention relates to coal chemical technology, especially relate to a kind of pure oxygen continuous gasification process.
Background technology
Fischer-tropsch reactor pure oxygen continuous gasification process is a kind of coal gasifying process, is mainly used in coal chemical technology, in ammonia synthesizing industry, chlorine industry, gas industry and coal-to-oil industry etc., all needs to use this technique.
The existing coal gasifying process in gasification field has pressing gas and normal pressure gas at present, the typical gasifying process of pressing gasization has SHELL gasification, GSP gasification, HT-L gasification and coal water slurry gasification, single stove production capacity of pressing gas is larger, investment is large, construction period is long, and main application fields is large-scale Coal Chemical Industry; Normal pressure gas metallization processes mainly contains the gasification of fixed-bed intermittent formula and fixed bed oxygen-enriched gasification.
Both advantages are that investment is little, and the construction period is short, produce load adjustment convenient.The shortcoming of fixed-bed intermittent formula gasification be have exhaust gas emission, efficiency of carbon conversion is low, the effective gas content of coal gas is low, technique falls behind, the equipment cycle of operation is short.Fixed bed oxygen-enriched gasifying process is compared and is had certain advance with batch process, but effective gas content of gas product is low, and range of application is little.So far, in coal gasifying process field, also do not have a kind of technique can meet following condition completely: non-exhaust emission, invest little, produce that load adjustment is convenient, effectively gas content is high, efficiency of carbon conversion is high, coal gas strong adaptability etc.
Summary of the invention
The object of the present invention is to provide a kind of fischer-tropsch reactor pure oxygen continuous gasification device and gasifying process, improve heat of gasification efficiency.
Technical scheme of the present invention is:
Fischer-tropsch reactor pure oxygen continuous gasification device, comprise coke charger, pure oxygen gasification stove, cyclonic separator, sensible heat recoverer, vaporized chemical preheater, mixing tank, the body of heater aspect ratio of pure oxygen gasification stove is 2.4 ~ 3.2, mixing tank is provided with oxygen intake and steam entry, mixing tank connects vaporized chemical preheater by pipeline, vaporized chemical preheater is connected with pure oxygen gasification stove by pipeline, the top of pure oxygen gasification stove connects coke charger, the top of pure oxygen gasification stove connects cyclonic separator by pipeline, cyclonic separator is connected with sensible heat recoverer, the bottom of sensible heat recoverer is connected with the bottom of vaporized chemical preheater by pipeline.
The bottom of pure oxygen gasification stove is provided with continuous deslagging device.
Fischer-tropsch reactor pure oxygen continuous gasification process flow process:
The first step: feed coal, in coke charger enters pure oxygen gasification stove, forms the stable bed of material in vapourizing furnace;
Second step: vaporized chemical oxygen and water vapor evenly mix in mixing tank, forms hybrid gasification agent, sends into through vaporized chemical preheater;
The 3rd step, utilizes waste-heat: the temperature that improves hybrid gasification agent after the heat exchange of vaporized chemical preheater;
The 4th step: the hybrid gasification agent after waste-heat enters pure oxygen gasification stove from the bottom of pure oxygen gasification stove, hybrid gasification agent reacts with red-hot carbon generating gasification, slag after gasification is discharged from the continuous deslagging device of pure oxygen gasification furnace bottom, and the coal gas of generation from pure oxygen gasification furnace roof portion out;
The 5th step: the gas product that goes out coal gas enters cyclonic separator, carries out separation to the coal dust in gas product;
The 6th step: the coal gas after the separated coal dust of cyclonic separator enters sensible heat recoverer, reclaims for the first time sensible heat;
The 7th step: enter vaporized chemical preheater from sensible heat recoverer low temperature coal gas out, reclaim for the second time sensible heat, send battery limit (BL) through the coal gas reclaiming for the second time after sensible heat.
In the first step, feed coal is heated to red-hot state, and temperature is 1000-1200 ℃.
In the 4th step, pure oxygen gasification furnace roof portion gas temperature is out 400-450 ℃.
In the 3rd step, after the heat exchange of vaporized chemical preheater, the temperature of hybrid gasification agent reaches 100-120 ℃.
The gas temperature of sending battery limit (BL) in the 7th step after reclaiming for the second time sensible heat should be less than 140 ℃.
Fischer-tropsch reactor pure oxygen continuous gasification process is a kind of novel gas metallization processes, belong to normal pressure continuous gasification process, technique of the present invention is invention and the innovation on original atmospheric gasification technique basis, carries out innovation aspect gasification furnace structure, makes it to be applicable to the process requirements of high gas temperature.In technical process, be optimized, make full use of the sensible heat of product gas product, to improve heat of gasification efficiency.The present invention has eliminated normal pressure gas metallization processes defect, non-exhaust emission, and effectively gas content is high, and than other normal pressure gas, effectively gas content can improve more than 10%.Compare pressing gas, it is little that the present invention has investment, instant effect, and thermo-efficiency is high, is applicable to the coal chemical industry enterprises of middle and small scale, flexible operation, easier stably manufactured load.
The present invention has the following advantages:
1, the application of continuously feeding and slag discharging device, guarantees continuous gasification, non-exhaust emission;
2, the advantage of vaporized chemical distribution apparatus is when being uniformly distributed vaporized chemical, reclaims the heat of vapourizing furnace bottom, improves vapourizing furnace thermo-efficiency.
3, body of heater aspect ratio (different according to coal, aspect ratio is controlled at 2.8-3.2); When aspect ratio is controlled within the scope of this, vapourizing furnace is more stable, and gasification efficiency is higher.
4, adopt secondary sensible heat recovery process, use battery limit (BL) gas temperature and be less than 140 ℃, guarantee higher gas furnace hot efficiency, effective use of energy sources.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention and schema.
Embodiment
As shown in Figure 1, the inventive system comprises coke charger 1, pure oxygen gasification stove 2, cyclonic separator 3, sensible heat recoverer 4, vaporized chemical preheater 5, mixing tank 6.The body of heater aspect ratio of pure oxygen gasification stove 2 is 2.4 ~ 3.2, and the gas temperature that guarantees out vapourizing furnace is 400-450 ℃.The bottom of pure oxygen gasification stove 2 is provided with continuous deslagging device 7 and vaporized chemical distribution apparatus 8.Feed coal can be anthracite block coal, can be also coke, can be also moulded coal.
Mixing tank 6 is provided with oxygen intake and steam entry, mixing tank 6 connects vaporized chemical preheater 5 by pipeline, the top of vaporized chemical preheater 5 is provided with pipeline and is connected with pure oxygen gasification stove 2, the top of pure oxygen gasification stove 2 connects coke charger 1, the top of pure oxygen gasification stove 2 connects cyclonic separator 3 by pipeline, cyclonic separator 3 is connected with sensible heat recoverer 4, and the bottom of sensible heat recoverer 4 is connected with the bottom of vaporized chemical preheater 5 by pipeline.Sensible heat recoverer 4 bottoms are provided with soft water water inlet pipe.
Fischer-tropsch reactor pure oxygen continuous gasification process flow process:
The first step: feed coal, in coke charger 1 enters pure oxygen gasification stove 2, forms the stable bed of material in vapourizing furnace.Carbon is heated to red-hot state.The temperature of red-hot state is 1000-1200 ℃.
Second step: vaporized chemical oxygen and water vapor, in the interior even mixing of mixing tank 6, form hybrid gasification agent, send into through vaporized chemical preheater 5;
The 3rd step, utilizes waste-heat.After 5 heat exchange of vaporized chemical preheater, the temperature of hybrid gasification agent is 100-120 ℃.Reduced gas temperature, gas recovery sensible heat simultaneously;
The 4th step: the hybrid gasification agent after waste-heat enters pure oxygen gasification stove 2 from the bottom of pure oxygen gasification stove 2, hybrid gasification agent reacts with red-hot carbon generating gasification, slag after gasification is discharged from the continuous deslagging device 7 of pure oxygen gasification stove 2 bottoms, from pure oxygen gasification stove 2 tops out, now gas temperature is 400-450 ℃ to the coal gas producing;
The 5th step: the gas product that goes out coal gas enters cyclonic separator 3, and the coal dust in gas product is carried out to separation;
The 6th step: the coal gas after the separated coal dust of cyclonic separator 3 enters sensible heat recoverer 4, reclaims for the first time sensible heat;
The 7th step: enter vaporized chemical preheater 5 from sensible heat recoverer 4 low temperature coal gas out, reclaim for the second time sensible heat, send battery limit (BL) through the coal gas reclaiming for the second time after sensible heat, the gas temperature that can use battery limit (BL) is less than 140 ℃.
In technological process of the present invention the 3rd step, during 5 heat exchange of vaporized chemical preheater, coal gas enters vaporized chemical preheater 5 from sensible heat recoverer 4 low temperature coal gas out, and heat is provided.
The adaptability to raw material of technique of the present invention is wide, can be anthracite block coal, can be also coke, can be also moulded coal, can be applied to multiple Coal Chemical Industry industry.Different according to coal, can transform existing intermittent type gasification, also can be newly-built.In the situation that not affecting production, can progressively replace and pollute the backward gasifying process device large, energy consumption is high, to increase economic efficiency and environmental benefit.
Claims (7)
1. fischer-tropsch reactor pure oxygen continuous gasification device, it is characterized in that: comprise coke charger, pure oxygen gasification stove, cyclonic separator, sensible heat recoverer, vaporized chemical preheater, mixing tank, the body of heater aspect ratio of pure oxygen gasification stove is 2.4 ~ 3.2, mixing tank is provided with oxygen intake and steam entry, mixing tank connects vaporized chemical preheater by pipeline, vaporized chemical preheater is connected with pure oxygen gasification stove by pipeline, the top of pure oxygen gasification stove connects coke charger, the top of pure oxygen gasification stove connects cyclonic separator by pipeline, cyclonic separator is connected with sensible heat recoverer, the bottom of sensible heat recoverer is connected with the bottom of vaporized chemical preheater by pipeline.
2. fischer-tropsch reactor pure oxygen continuous gasification device according to claim 1, is characterized in that: the bottom of pure oxygen gasification stove is provided with continuous deslagging device.
3. the gasifying process that adopts the fischer-tropsch reactor pure oxygen continuous gasification device described in claim 1 or 2, is characterized in that: fischer-tropsch reactor pure oxygen continuous gasification process flow process:
The first step: feed coal, in coke charger enters pure oxygen gasification stove, forms the stable bed of material in vapourizing furnace;
Second step: vaporized chemical oxygen and water vapor evenly mix in mixing tank, forms hybrid gasification agent, sends into through vaporized chemical preheater;
The 3rd step, utilizes waste-heat: the temperature that improves hybrid gasification agent after the heat exchange of vaporized chemical preheater;
The 4th step: the hybrid gasification agent after waste-heat enters pure oxygen gasification stove from the bottom of pure oxygen gasification stove, hybrid gasification agent reacts with red-hot carbon generating gasification, slag after gasification is discharged from the continuous deslagging device of pure oxygen gasification furnace bottom, and the coal gas of generation from pure oxygen gasification furnace roof portion out;
The 5th step: the gas product that goes out coal gas enters cyclonic separator, carries out separation to the coal dust in gas product;
The 6th step: the coal gas after the separated coal dust of cyclonic separator enters sensible heat recoverer, reclaims for the first time sensible heat;
The 7th step: enter vaporized chemical preheater from sensible heat recoverer low temperature coal gas out, reclaim for the second time sensible heat, send battery limit (BL) through the coal gas reclaiming for the second time after sensible heat.
4. fischer-tropsch reactor pure oxygen continuous gasification process according to claim 3, is characterized in that: in the first step, feed coal is heated to red-hot state, and temperature is 1000-1200 ℃.
5. according to the fischer-tropsch reactor pure oxygen continuous gasification process described in claim 3 or 4, it is characterized in that: in the 4th step, pure oxygen gasification furnace roof portion gas temperature is out 400-450 ℃.
6. according to the fischer-tropsch reactor pure oxygen continuous gasification process described in claim 3 or 4, it is characterized in that: in the 3rd step, after the heat exchange of vaporized chemical preheater, the temperature of hybrid gasification agent reaches 100-120 ℃.
7. according to the fischer-tropsch reactor pure oxygen continuous gasification process described in claim 3 or 4, it is characterized in that: the gas temperature of sending battery limit (BL) in the 7th step after reclaiming for the second time sensible heat should be less than 140 ℃.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104789266A (en) * | 2015-03-23 | 2015-07-22 | 七台河宝泰隆煤化工股份有限公司 | Coal gas generating method |
| CN105349186A (en) * | 2015-12-11 | 2016-02-24 | 山东百川同创能源有限公司 | Biomass gas making system and biomass gas making technology based on microwave heating |
| CN114410352A (en) * | 2022-02-24 | 2022-04-29 | 安徽科达洁能股份有限公司 | Adjustable waste heat recovery device and method |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104789266A (en) * | 2015-03-23 | 2015-07-22 | 七台河宝泰隆煤化工股份有限公司 | Coal gas generating method |
| CN105349186A (en) * | 2015-12-11 | 2016-02-24 | 山东百川同创能源有限公司 | Biomass gas making system and biomass gas making technology based on microwave heating |
| CN105349186B (en) * | 2015-12-11 | 2019-03-05 | 山东百川同创能源有限公司 | Biogas system and technique based on microwave heating |
| CN114410352A (en) * | 2022-02-24 | 2022-04-29 | 安徽科达洁能股份有限公司 | Adjustable waste heat recovery device and method |
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