CN202610195U - Device for preparing ammonia synthesis gas through pressurization and continuous gasification of anthracite - Google Patents
Device for preparing ammonia synthesis gas through pressurization and continuous gasification of anthracite Download PDFInfo
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- CN202610195U CN202610195U CN2012202563248U CN201220256324U CN202610195U CN 202610195 U CN202610195 U CN 202610195U CN 2012202563248 U CN2012202563248 U CN 2012202563248U CN 201220256324 U CN201220256324 U CN 201220256324U CN 202610195 U CN202610195 U CN 202610195U
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Abstract
The utility model discloses a device for preparing ammonia synthesis gas through pressurization and continuous gasification of anthracite with oxygen-enriched air, belonging to the technical field of preparation of the ammonia through gasification of an anthracite-pressurized movable bed. The technical problem to be solved is as follows: an ammonia synthesis gas device, which adopts the oxygen-enriched air and saturated steam as gasifying agents and is capable of continuously pressurizing and gasifying small-size anthracite, is provided; the technical scheme is as follows: the air inlet of a preheating furnace is connected with the air outlet of an the oxygen-enriched air compressor, the air outlet of the preheating furnace is connected with the air inlet of a gasification furnace, the air outlet of the gasification furnace is connected with the air inlet of a separator, the air outlet of the separator is connected with the air inlet of a boiler, the air outlet of the boiler is connected with the air inlet of a Venturi dust collector, the air outlet of the Venturi dust collector is connected with the air inlet of a washing tower, and the air outlet of the washing tower is connected with the air inlet of a low-pressure waste heat boiler. The device, provided by the utility model, is widely applied to the field of preparation of ammonia synthesis gas through continuous gasification of the anthracite.
Description
Technical field
The utility model hard coal pressurization oxygen-rich air continuous gasification prepares the ammonia synthesis gas device, belongs to hard coal pressurization moving-bed gasification and prepares the ammonia technical field.
Background technology
China was 5068.7 ten thousand tons of raw material production synthetic ammonia with the coal in 2011, and it is about 65% wherein to adopt synthetic ammonia ability that the thirties in 20th century, atmosphere intermission technology was produced to account for, the main shortcoming that this technology exists:
1, require that sulphur content is low, active high, ash fusion point is high, Heat stability is good, physical strength is high, clinkering property is weak, anthracite block coal or the coke of 25-75mm.Therefore the feed coal limitation is very strong, and the utilization ratio of coal is very low, the one-tenth piece rate of 25-75mm only 15%.Price per ton is up to more than 1200 yuan.Most of enterprise is in the edge of loss or loss.
2, atmospheric gasification makes coal gas does not have pressure, and ammonia synthesis requires the very high 15-30Mpa of pressure, and therefore, compression work increases greatly, compares the many 300kW of ammonia power consumption per ton with the 4MPa pressurized gasification.And the gasification intensity of atmospheric gasification is very low, and the vapourizing furnace quantity that needs is many more than 4 times.
3, gasify in traditional gap, the coal of blowing stage burning process consumption accounts for 40%, and the blowing air of generation all enters atmosphere after waste thermal energy reclaims, and 40% sulphur is with SO in the coal
2, nitrogen NO
xForm enters atmosphere.With Jincheng hard coal is example, low sulphur coal mean content of sulfur 0.8%, and nitrogen about 0.7%, then annual to airborne release SO
2800,000 tons, a certain amount of NO
xThis shows, atmosphere is caused severe contamination.
4, energy consumption is high, blowing efficient only 39%, and cold gas efficiency 62%, steam decomposition rate 50%, even will contain charcoal 15-20%, moisture lime-ash more than 30%, the gas making ash of carbon containing 50% flies to send burning in boiler, and its calorific value is also lower than coal gangue, and utility value is limited.
There is abundant anthracite resource in China, and its ature of coal characteristic: sulphur content 0.5-3%, ash content are relatively poor greater than 1500 ℃, the special difficult mill of coal of grindability index about 35, coal activity up to 18-24%, ash fusion point, should not use what air flow bed, fluidized bed gasifying process.Have only broken coal pressurization pure oxygen gasification comparatively suitable, but oxygen consumes height, steam decomposition rate is low less than 35-38%, 650-700 ℃ coal gas of high temperature is produced the 0.6Mpa low-pressure saturated steam through water washing to 206 ℃ entering waste heat boiler, reduces the utilization ratio of ability.Steam consumption is big, steam decomposition rate is low, and wastewater flow rate is big, and cost is high, limits this technology and applies.Because some areas, the year-end intact energy-saving index that does not become country to assign is compelled this class factory is closed.Therefore country expressly provides, does not allow and adopts the new factory of fixed bed intermittent gasification Technology construction, and require these old factories are quickened to transform and make pottery and eliminate.
Summary of the invention
The utility model is in order to overcome the deficiency of prior art, and it is vaporized chemical that a kind of employing oxygen-rich air and saturation steam are provided, continuously the anthracitic ammonia synthesis gas device in pressurized gasification fritter footpath.
In order to solve the problems of the technologies described above; The technical scheme that the utility model adopts is: hard coal pressurization continuous gasification prepares the ammonia synthesis gas device; Comprise oxygen-rich air compressor, preheating oven, vapourizing furnace, vapourizing furnace drum, high temperature cyclone separator, waste heat boiler, waste heat boiler drum, venturi scrubber, washing tower and Low Pressure Waste Heat Boiler and Low Pressure Waste Heat Boiler drum, said preheating oven side is provided with preheating oven inlet mouth, preheating oven air outlet, preheating oven water-in and preheating oven water outlet; Said top of gasification furnace is provided with coal lock bucket, and the bottom is provided with ash lock bucket, and the side is provided with vapourizing furnace inlet mouth, vapourizing furnace water-in, vapourizing furnace water outlet and vapourizing furnace air outlet; Said high temperature cyclone separator top is provided with the separator air outlet, and the bottom is provided with the separator dust mouth, and the side is provided with the separator inlet mouth; Said waste heat boiler top is provided with the boiler inlet mouth, and the bottom is provided with the boiler dust mouth, and the side is provided with boiler feed water mouth, boiler water outlet and boiler air outlet; Said washing tower top is provided with the washing tower air outlet, and the bottom is provided with the washing tower water outlet, and the side is provided with washing tower water-in and washing tower inlet mouth; Said Low Pressure Waste Heat Boiler top is provided with the low pressure boiler inlet mouth, and the bottom is provided with the low pressure boiler air outlet, and the side is provided with low pressure boiler water-in and low pressure boiler water outlet;
Said preheating oven inlet mouth links to each other with the oxygen-rich air compressor outlet; The preheating oven air outlet links to each other with the vapourizing furnace inlet mouth; The vapourizing furnace air outlet links to each other with the separator inlet mouth, and the separator air outlet links to each other with the boiler inlet mouth, and the boiler air outlet links to each other with the venturi scrubber inlet mouth; The venturi scrubber air outlet links to each other with the washing tower inlet mouth, and the washing tower air outlet links to each other with the Low Pressure Waste Heat Boiler inlet mouth;
Said preheating oven water outlet links to each other with vapourizing furnace drum first water inlet, waste heat boiler drum first water inlet and Low Pressure Waste Heat Boiler drum first water inlet;
Vapourizing furnace drum second water inlet links to each other with the vapourizing furnace water outlet, and vapourizing furnace drum water outlet links to each other with the vapourizing furnace water inlet, and vapourizing furnace drum vapour outlet links to each other with the vapourizing furnace inlet mouth;
Waste heat boiler drum second water inlet links to each other with the boiler water outlet, and waste heat boiler drum water outlet links to each other with the boiler feed water mouth, and waste heat boiler drum vapour outlet links to each other with the preheating oven inlet mouth;
Low Pressure Waste Heat Boiler drum second water inlet links to each other with the low pressure boiler water outlet, and Low Pressure Waste Heat Boiler drum water outlet links to each other with the low pressure boiler water-in.
The utility model compared with prior art has following beneficial effect.
1, to adopt low-sulfur or the high-sulfur of 5-40mm, high ash, high ash melting point, the smokeless broken coal of difficult mill be raw material to the utility model, and the utilization ratio of coal is estimated from 15% to bring up to about 65%, estimates 800 yuan/ton of 5-40mm coal prices, so can reduce product cost greatly.
2, the utility model adopts the gasification of oxygen concn 45%-55% oxygen-rich air, raw gas through conversion, remove CO
2After, N
2: H
2=1:3 is used for ammonia synthesis; Because adopt the gasification of oxygen concn 48%-52% oxygen-rich air, air is brought 21% oxygen into; Because N in the oxygen-rich air
2Instead of part steam heat-carrying, steam and oxygen ratio drop to about 2.1 from 3.1, with similar pure oxygen gasification ratio, can reduce 30-35%; Oxygen consumption can reduce 25-28%, and steam consumption reduces 30-35%, reduces gas condensed water and handles 30-35%.
3, the utility model vapor pressure is 4Mpa, and the vapourizing furnace ability improves 4-5 doubly, because of gasification intensity is directly proportional with the square root of pressure; Vapourizing furnace quantity is merely 1/4 ~ 1/5 of atmospheric gasification; For device, factory maximize and create conditions, saved investment, reduced cost.
4, the waste gas that utilizes synthesis ammonia system to discharge is used for preheating oven, and the 4.8Mpa saturation steam of oxygen-rich air, the useless pot of gasification by-product is preheated to 500 ℃, produces with the vapourizing furnace chuck and goes into vapourizing furnace after the 4.2Mpa saturation steam mixes.Vapourizing furnace outlet raw gas; About pressure 4Mpa, 650-700 ℃, behind high-temperature cyclone dust extractor, get into waste heat boiler and produce the 4.8Mpa saturation steam, raw gas gets into water wash column for about 250 ℃ then; Temperature is reduced to 180 ℃; Saturated coal gas gets into changing device, the required steam of the enough transformationreations of its steam vapour amount of bringing into, and the energy utilization is very effectively.
Description of drawings
Below in conjunction with accompanying drawing the utility model is done further explanation.
Fig. 1 is the process structure synoptic diagram of the utility model.
1 is that oxygen-rich air compressor, 2 is that preheating oven, 3 is that vapourizing furnace, 4 is that vapourizing furnace drum, 5 is that high temperature cyclone separator, 6 is that waste heat boiler, 7 is that waste heat boiler drum, 8 is that venturi scrubber, 9 is that washing tower, 10 is that Low Pressure Waste Heat Boiler, 11 is the Low Pressure Waste Heat Boiler drum among the figure.
Embodiment
As shown in Figure 1; Hard coal pressurization continuous gasification prepares the ammonia synthesis gas device; Comprise oxygen-rich air compressor 1, preheating oven 2, vapourizing furnace 3, vapourizing furnace drum 4, high temperature cyclone separator 5, waste heat boiler 6, waste heat boiler drum 7, venturi scrubber 8, washing tower 9 and Low Pressure Waste Heat Boiler 10 and Low Pressure Waste Heat Boiler drum 11, it is characterized in that said preheating oven 2 sides are provided with preheating oven inlet mouth, preheating oven air outlet, preheating oven water-in and preheating oven water outlet; Said vapourizing furnace 3 tops are provided with coal lock bucket, and the bottom is provided with ash lock bucket, and the side is provided with vapourizing furnace inlet mouth, vapourizing furnace water-in, vapourizing furnace water outlet and vapourizing furnace air outlet; Said high temperature cyclone separator 5 tops are provided with the separator air outlet, and the bottom is provided with the separator dust mouth, and the side is provided with the separator inlet mouth; Said waste heat boiler 6 tops are provided with the boiler inlet mouth, and the bottom is provided with the boiler dust mouth, and the side is provided with boiler feed water mouth, boiler water outlet and boiler air outlet; Said washing tower 9 tops are provided with the washing tower air outlet, and the bottom is provided with the washing tower water outlet, and the side is provided with washing tower water-in and washing tower inlet mouth; Said Low Pressure Waste Heat Boiler 10 tops are provided with the low pressure boiler inlet mouth, and the bottom is provided with the low pressure boiler air outlet, and the side is provided with low pressure boiler water-in and low pressure boiler water outlet;
Said preheating oven inlet mouth links to each other with the oxygen-rich air compressor outlet; The preheating oven air outlet links to each other with the vapourizing furnace inlet mouth; The vapourizing furnace air outlet links to each other with the separator inlet mouth, and the separator air outlet links to each other with the boiler inlet mouth, and the boiler air outlet links to each other with the venturi scrubber inlet mouth; The venturi scrubber air outlet links to each other with the washing tower inlet mouth, and the washing tower air outlet links to each other with the Low Pressure Waste Heat Boiler inlet mouth;
Said preheating oven water outlet links to each other with vapourizing furnace drum first water inlet, waste heat boiler drum first water inlet and Low Pressure Waste Heat Boiler drum first water inlet;
Vapourizing furnace drum second water inlet links to each other with the vapourizing furnace water outlet, and vapourizing furnace drum water outlet links to each other with the vapourizing furnace water inlet, and vapourizing furnace drum vapour outlet links to each other with the vapourizing furnace inlet mouth;
Waste heat boiler drum second water inlet links to each other with the boiler water outlet, and waste heat boiler drum water outlet links to each other with the boiler feed water mouth, and waste heat boiler drum vapour outlet links to each other with the preheating oven inlet mouth;
Low Pressure Waste Heat Boiler drum second water inlet links to each other with the low pressure boiler water outlet, and Low Pressure Waste Heat Boiler drum water outlet links to each other with the low pressure boiler water-in.
Pure oxygen and air are fed oxygen-rich air compressor 1; Mix the boil down to oxygen-rich air; The oxygen level of said oxygen-rich air is 45%-55%, then oxygen-rich air is mixed with saturation steam from waste heat boiler 6, gets into preheating oven 2; Be preheated to the steam that produces with chuck after 500 ℃ and obtain virgin gas, the weight part ratio of steam and simple substance oxygen is 2-2.2:1 in the said virgin gas; Preheating oven 2 also will be supplied with the oiler feed preheating of vapourizing furnace drum 4, waste heat boiler drum 7 and Low Pressure Waste Heat Boiler drum 11 simultaneously.
The hard coal of piece footpath 5-40mm, sulphur content 0.5-3%, ash content 18-24%, 1450 ℃-1500 ℃ of ash fusion points, grindability index 32-50 gets into vapourizing furnace 3 through coal lock bucket, ash lock bucket; The coal gas counter current contact of hard coal and rising; Through super-dry, gasification, burning, clinker area, enter ash lock bucket and ash treatment system from top to bottom through the rotation grate.Oxygen-rich air compression back is mixed into preheating oven 2 with steam; Being preheated to 500 ℃ produces steam with chuck and mixes; Get into vapourizing furnace grate chambers 3; Ratio in setting is evenly distributed to vapourizing furnace 3 clinker areas, vaporized chemical and lime-ash heat exchange, and ash temperature drops to 300-350 ℃ from 1400-1450 ℃ and enters ash lock bucket.Gasification agent temperature further improves, and rises to the carbon residue burning that combustion zone and gasification reaction district move down, and temperature moment rising gets into the gasification zone for about 1450 ℃.Along with the carrying out of gasification reaction, gas temperature progressively descends until gasification reaction near stopping.The hard coal of oxygen-rich air every cubic metre (normal temperature and pressure) gasification 0.75-0.9kg in the gasification reaction, virgin gas and smokeless coal gasification reaction back generation raw gas, said raw gas pressure 4.0Mpa, temperature 650-700 ℃, raw gas is formed as follows:
| Component | CO | CO 2 | H 2 | CH 4 | N 2 | S |
| Volume percent % | 26-28 | 18-20 | 34-36 | 2-3 | 18-20 | 0.3-1 |
Raw gas feeds after high temperature cyclone separator 5 separates dedustings, feeds waste heat boiler 6 again and is cooled to 230-260 ℃, and the raw gas of once being lowered the temperature produces the high-pressure saturated steam of 4.8Mpa simultaneously, and said high-pressure saturated steam is used for mixing with said oxygen-rich air.
The said raw gas of once lowering the temperature is through venturi scrubber 8 once more after the dedusting; Get into washing tower 9 dedustings and be cooled to 206 ℃; Get into the ammonia synthesis raw gas that Low Pressure Waste Heat Boiler 10 reducing temperature twices obtain 170-190 ℃ at last; Produce the 0.6Mpa LP steam simultaneously, the contained saturation steam of said ammonia synthesis raw gas satisfies the conversion condition.
Because synthetic ammonia needs 25% nitrogen, therefore adopt oxygen-rich air gasification under the 4Mpa pressure, ammonia power consumption per ton can reduce more than the 300kw.Go into the stove coal particle size and become 5-50mm from 25-75mm, utilization ratio brings up to 65% from 15%.The feed coal cost can reduce more than 40%.Can reduce oxygen consumption 25-28%, steam consumption reduces 30-35%, reduces gas condensed water and handles 30-35%.
Adopt the gasification of oxygen concn 45%-55% oxygen-rich air, raw gas through conversion, remove CO
2After, N
2: H
2=1:3 is used for ammonia synthesis.
Because adopt the gasification of oxygen concn 45%-55% oxygen-rich air, air is brought 21% oxygen into, the oxygen consumption reduces 25-28%.
Because N in the oxygen-rich air
2Instead of part steam heat-carrying, with similar pure oxygen gasification ratio, steam consumption can reduce 30-35%.
Claims (1)
1. hard coal pressurization continuous gasification prepares the ammonia synthesis gas device; Comprise oxygen-rich air compressor (1), preheating oven (2), vapourizing furnace (3), vapourizing furnace drum (4), high temperature cyclone separator (5), waste heat boiler (6), waste heat boiler drum (7), venturi scrubber (8), washing tower (9) and Low Pressure Waste Heat Boiler (10) and Low Pressure Waste Heat Boiler drum (11), it is characterized in that said preheating oven (2) side is provided with preheating oven inlet mouth, preheating oven air outlet, preheating oven water-in and preheating oven water outlet; Said vapourizing furnace (3) top is provided with coal lock bucket, and the bottom is provided with ash lock bucket, and the side is provided with vapourizing furnace inlet mouth, vapourizing furnace water-in, vapourizing furnace water outlet and vapourizing furnace air outlet; Said high temperature cyclone separator (5) top is provided with the separator air outlet, and the bottom is provided with the separator dust mouth, and the side is provided with the separator inlet mouth; Said waste heat boiler (6) top is provided with the boiler inlet mouth, and the bottom is provided with the boiler dust mouth, and the side is provided with boiler feed water mouth, boiler water outlet and boiler air outlet; Said washing tower (9) top is provided with the washing tower air outlet, and the bottom is provided with the washing tower water outlet, and the side is provided with washing tower water-in and washing tower inlet mouth; Said Low Pressure Waste Heat Boiler (10) top is provided with the low pressure boiler inlet mouth, and the bottom is provided with the low pressure boiler air outlet, and the side is provided with low pressure boiler water-in and low pressure boiler water outlet;
Said preheating oven inlet mouth links to each other with the oxygen-rich air compressor outlet; The preheating oven air outlet links to each other with the vapourizing furnace inlet mouth; The vapourizing furnace air outlet links to each other with the separator inlet mouth, and the separator air outlet links to each other with the boiler inlet mouth, and the boiler air outlet links to each other with the venturi scrubber inlet mouth; The venturi scrubber air outlet links to each other with the washing tower inlet mouth, and the washing tower air outlet links to each other with the Low Pressure Waste Heat Boiler inlet mouth;
Said preheating oven water outlet links to each other with vapourizing furnace drum first water inlet, waste heat boiler drum first water inlet and Low Pressure Waste Heat Boiler drum first water inlet;
Vapourizing furnace drum second water inlet links to each other with the vapourizing furnace water outlet, and vapourizing furnace drum water outlet links to each other with the vapourizing furnace water inlet, and vapourizing furnace drum vapour outlet links to each other with the vapourizing furnace inlet mouth;
Waste heat boiler drum second water inlet links to each other with the boiler water outlet, and waste heat boiler drum water outlet links to each other with the boiler feed water mouth, and waste heat boiler drum vapour outlet links to each other with the preheating oven inlet mouth;
Low Pressure Waste Heat Boiler drum second water inlet links to each other with the low pressure boiler water outlet, and Low Pressure Waste Heat Boiler drum water outlet links to each other with the low pressure boiler water-in.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103509605A (en) * | 2013-10-13 | 2014-01-15 | 上海穗杉实业有限公司 | Method and device using high temperature air and high temperature steam as gasification agents for coal gas production |
| CN104403691A (en) * | 2014-12-11 | 2015-03-11 | 赛鼎工程有限公司 | Technology and device for preparing clean fuel gas from crushed coal slag gasified coal |
| CN104403692A (en) * | 2014-12-11 | 2015-03-11 | 赛鼎工程有限公司 | Technology and equipment for producing clean gas by gasifying broken molten coal slag |
| CN104593081A (en) * | 2014-12-11 | 2015-05-06 | 赛鼎工程有限公司 | Process and device for production of clean fuel gas from coal |
| CN104893762A (en) * | 2015-06-15 | 2015-09-09 | 林兆晟 | Raw gas ash handling system |
| CN106545831A (en) * | 2017-01-24 | 2017-03-29 | 北京金泰瑞和工程科技有限公司 | Waste heat boiler heat exchanger and fixed bed pressured gasification system |
| CN107201250A (en) * | 2017-05-19 | 2017-09-26 | 山西晋煤集团技术研究院有限责任公司 | A kind of utilization anthracite prepares device and method of the glass furnace with hot fuel gas |
| CN107828449A (en) * | 2017-11-08 | 2018-03-23 | 中科合肥煤气化技术有限公司 | A kind of device for reclaiming gasification furnace coal gas of high temperature heat |
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2012
- 2012-06-01 CN CN2012202563248U patent/CN202610195U/en not_active Expired - Lifetime
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103509605A (en) * | 2013-10-13 | 2014-01-15 | 上海穗杉实业有限公司 | Method and device using high temperature air and high temperature steam as gasification agents for coal gas production |
| CN104403691A (en) * | 2014-12-11 | 2015-03-11 | 赛鼎工程有限公司 | Technology and device for preparing clean fuel gas from crushed coal slag gasified coal |
| CN104403692A (en) * | 2014-12-11 | 2015-03-11 | 赛鼎工程有限公司 | Technology and equipment for producing clean gas by gasifying broken molten coal slag |
| CN104593081A (en) * | 2014-12-11 | 2015-05-06 | 赛鼎工程有限公司 | Process and device for production of clean fuel gas from coal |
| CN104403691B (en) * | 2014-12-11 | 2016-06-08 | 赛鼎工程有限公司 | The technique of a kind of broken coal slag gasification of coal clean gas and device |
| CN104403692B (en) * | 2014-12-11 | 2016-08-24 | 赛鼎工程有限公司 | The gasification of broken coal slag produces the Processes and apparatus of clean gas |
| CN104593081B (en) * | 2014-12-11 | 2017-01-04 | 赛鼎工程有限公司 | The technique of coal clean gas and device |
| CN104893762A (en) * | 2015-06-15 | 2015-09-09 | 林兆晟 | Raw gas ash handling system |
| CN104893762B (en) * | 2015-06-15 | 2017-07-14 | 林兆晟 | Raw gas ash disposal system |
| CN106545831A (en) * | 2017-01-24 | 2017-03-29 | 北京金泰瑞和工程科技有限公司 | Waste heat boiler heat exchanger and fixed bed pressured gasification system |
| CN107201250A (en) * | 2017-05-19 | 2017-09-26 | 山西晋煤集团技术研究院有限责任公司 | A kind of utilization anthracite prepares device and method of the glass furnace with hot fuel gas |
| CN107828449A (en) * | 2017-11-08 | 2018-03-23 | 中科合肥煤气化技术有限公司 | A kind of device for reclaiming gasification furnace coal gas of high temperature heat |
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Granted publication date: 20121219 |