CN102743889B - Liquid ammonia evaporator and liquid ammonia evaporation system for flue gas denitration - Google Patents
Liquid ammonia evaporator and liquid ammonia evaporation system for flue gas denitration Download PDFInfo
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- CN102743889B CN102743889B CN201210249329.2A CN201210249329A CN102743889B CN 102743889 B CN102743889 B CN 102743889B CN 201210249329 A CN201210249329 A CN 201210249329A CN 102743889 B CN102743889 B CN 102743889B
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Abstract
The invention discloses a liquid ammonia evaporator and a liquid ammonia evaporation system for flue gas denitration, wherein the liquid ammonia evaporator comprises a heat exchange chamber and a stainless steel heat exchange pipe which is arranged in the heat exchange chamber; the heat exchange chamber consists of a lower heat exchange chamber and an upper heat exchange chamber; a denitrated flue gas inlet is arranged at the top of the lower heat exchange chamber and a denitrated flue gas outlet is arranged at the bottom of the lower heat exchange chamber; a hot air inlet is arranged at the bottom of the upper heat exchange chamber and a hot air outlet is arranged at the top of the upper heat exchange chamber; the stainless steel heat exchange pipe comprises a primary heat exchange pipe which is arranged in the lower heat exchange chamber and a secondary evaporator heat exchange pipe which is arranged in the upper heat exchange chamber; the pipe wall of the secondary evaporator heat exchange pipe consists of an inner wall and an outer wall; evenly distributed millimeter-level small holes are arranged on the inner wall; and evenly distributed micron-level micro holes are arranged on the outer wall, according to the liquid ammonia evaporator, the heat exchange efficiency of liquid ammonia is greatly improved and an ammonia evaporation supply system is simplified; and the liquid ammonia evaporation system has a compact structure and is capable of fully utilizing the waste heat of flue gas and the heat of preheated air.
Description
Technical field
The present invention relates to a kind of liquid ammonia evaporator and ammonia evaporation supply system being applied in denitrating flue gas field.
Background technology
SCR (selective catalytic reduction) denitrating technique is the main denitrating technique of current coal-burning power plant, its principle is under the effect of uniform temperature and catalyst, and reducing agent is selectively reduced to free of contamination N2 and water the NOx in flue gas.The reducing agent of commercial Application is mainly ammonia at present, next is urea, wherein adopt ammonia need to use ammonia evaporation supply system as reducing agent, first liquefied ammonia is evaporated to ammonia, then by ammonia surge tank, and then mix in blender with air (utilizing dilution air to carry), and then enter ammonia-spraying grid, finally enter again catalytic reactor and react.
Traditional ammonia evaporation supply system comprises the equipment such as liquid ammonia evaporator, ammonia surge tank, ammonia dilution trap, dilution air, and the evaporation supply system of ammonia adopts Steam Heating or coil pipe heating water bath more, no matter adopt in addition steam or heating water bath, be equipped with dump pipeline, unnecessary ammonia will, by dump discharge of pipes to absorbing pond, finally drain into waste plant and process.Traditional ammonia evaporation supply system flow process is complicated, and heat exchange efficiency is low, and needs extra steam or heat, so need to improve.
Summary of the invention
The object of this invention is to provide a kind of technique is simple, heat exchange efficiency the is high liquid ammonia evaporator for denitrating flue gas and liquefied ammonia vapo(u)rization system, solve traditional ammonia evaporation supply system complex structure, heat exchange efficiency is low and need extra steam or the technical problem of heat.
For achieving the above object, the present invention adopts following technical scheme: a kind of liquid ammonia evaporator for denitrating flue gas, comprise Heat Room and be located at the stainless steel heat exchange tube in Heat Room, it is characterized in that: described Heat Room is comprised of bottom Heat Room and top Heat Room, the top of bottom Heat Room has denitration gas approach, the bottom of bottom Heat Room has denitration exhanst gas outlet, and the bottom of top Heat Room has hot-air inlets, and the top of top Heat Room has hot air outlet.
Described stainless steel heat exchange tube comprises the heat exchanger tube being located in the Heat Room of bottom and is located at the revaporizer heat exchanger tube in the Heat Room of top, and No. one time heat exchanger tube is communicated with revaporizer heat exchanger tube, the tube wall of described revaporizer heat exchanger tube is comprised of inner and outer wall, wherein inwall is provided with equally distributed millimetre-sized aperture, and outer wall is provided with equally distributed micron-sized micropore.
The entrance point of a described heat exchanger tube is communicated with the lower straighttube that is positioned at the level of Heat Room bottom, bottom, on lower straighttube, have the liquefied ammonia import that is communicated with use with liquefied ammonia feed-line, the entrance point of described revaporizer heat exchanger tube is communicated with the upper straight tube that is positioned at the level of Heat Room bottom, top, upper straight tube is communicated with the port of export of a heat exchanger tube again, and the port of export of revaporizer heat exchanger tube is communicated with the revaporizer gathering tube that is positioned at the level at Heat Room top, top.
The caliber of described lower straighttube can be 4～5 times of caliber of liquefied ammonia feed-line, and the caliber of upper straight tube can be 6～8 times of caliber of liquefied ammonia feed-line.
A described heat exchanger tube can be snakelike tube fin type heat exchange pipe.
The caliber of described tube fin type heat exchange pipe can be 15mm～25mm, and the fin height of tube fin type heat exchange pipe can be 50%～60% of caliber, and the spacing of fin can be 2.5mm～3.5mm, and the spacing between tube fin type heat exchange pipe can be 30mm～50mm.
The interface of described tube fin type heat exchange pipe and lower straighttube is horizontal interface or vertical joint, and the center line of all tube fin type heat exchange pipes and the interface of lower straighttube is in same level.
Described revaporizer heat exchanger tube can be the vertical tube that many parallel interval arrange.
The thickness of the inwall in described vertical tube can be 10 mm～15mm, and the aperture of the aperture on inwall can be 1mm～3mm, and the aperture of the micropore on outer wall can be 5um～10um.
The percent opening of described outer wall can be 1%～5%.
A kind of liquefied ammonia vapo(u)rization system for denitrating flue gas, include liquid ammonia storage tank, liquid ammonia evaporator and ammonia-spraying grid, wherein liquid ammonia evaporator comprises Heat Room and is located at the stainless steel heat exchange tube in Heat Room, liquid ammonia storage tank is communicated with the stainless steel heat exchange tube in liquid ammonia evaporator by liquefied ammonia feed-line, in the exhaust gases passes of ammonia-spraying grid between boiler and catalytic reactor, it is characterized in that: described liquid ammonia evaporator is the above-mentioned liquid ammonia evaporator for denitrating flue gas, denitration gas approach on liquid ammonia evaporator enters boiler channel by flue gas and is communicated with the exhaust gases passes between air preheater with catalytic reactor, denitration exhanst gas outlet on liquid ammonia evaporator goes out boiler channel by flue gas and is communicated with the exhaust gases passes between exhanst gas outlet with air preheater, hot-air inlets on liquid ammonia evaporator is communicated with the air duct between boiler with air preheater by air branch road, hot air outlet on liquid ammonia evaporator is communicated with ammonia-spraying grid by mixed gas passage.
Compared with prior art the present invention has following characteristics and beneficial effect: the liquid ammonia evaporator in the present invention has adopted integrated design, traditional liquid ammonia evaporator is combined with diffusion release, fin-tube type gas-liquid heat exchange is combined with direct heat transfer, so greatly improved the heat exchange efficiency of liquefied ammonia, simplified ammonia evaporation supply system.
Liquefied ammonia vapo(u)rization system employing discharged gas fume in the present invention and the air after preheating, as thermal source and carrier gas, have reduced the consumption of steam or other energy.Simultaneously liquefied ammonia vapo(u)rization system utilized flue gas and preheating the pressure differential of air, do not need external motive device, easy maintenance.
Liquefied ammonia vapo(u)rization system compact conformation in the present invention, heat exchange efficiency is high, can make full use of the heat of fume afterheat and preheated air, and the heat exchange of liquefied ammonia, the mixing of ammonia all complete in liquid ammonia evaporator, so without ammonia emission, the atmosphere pollution of having avoided ammonia leakage to cause.
The present invention utilizes high-temperature flue gas as the main thermal source of liquefied ammonia evaporation, 100%～120% of institute's calorific requirement is provided, utilize the preheated air of process air preheater as supplemental heat source and the carrier gas of liquefied ammonia evaporation, the ammonia-spraying grid that directly enters catalytic unit through the ammonia of dilution reacts, and is applicable in SCR (SCR) flue-gas denitration process evaporation, release and mixing as the liquefied ammonia of reducing agent.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the present invention will be further described in detail.
Fig. 1 is the structural representation for the liquefied ammonia vapo(u)rization system of denitrating flue gas.
Fig. 2 is the structural representation for the liquid ammonia evaporator of denitrating flue gas.
Fig. 3 is the enlarged diagram at I place in Fig. 2.
Fig. 4 is the enlarged diagram at II place in Fig. 3.
Fig. 5 is the schematic diagram of A-A section in Fig. 2.
Fig. 6 is the schematic diagram of B-B section in Fig. 2.
Fig. 7 is the schematic diagram of C-C section in Fig. 2.
Reference numeral: 1-bottom Heat Room, 2-top Heat Room, 3-denitration gas approach, 4-denitration exhanst gas outlet, 5-hot-air inlets, 6-hot air outlet, heat exchanger tube of 7-, 8-lower straighttube, the import of 9-liquefied ammonia, the upper straight tube of 10-, 11-revaporizer heat exchanger tube, 12-inwall, 13-outer wall, 14-aperture, 15-micropore, 16-revaporizer gathering tube, 17-boiler, 18-economizer, exhaust gases passes between 19-boiler and catalytic reactor, 20-catalytic reactor, 21-flue gas enters boiler channel, 22-flue gas goes out boiler channel, air duct between 23-air intlet and air preheater, 24-air preheater, 25-air branch road, 26-mixed gas passage, 27-ammonia-spraying grid, 28-liquid ammonia storage tank, exhaust gases passes between 29-catalytic reactor and air preheater, exhaust gases passes between 30-air preheater and exhanst gas outlet, air duct between 31-air preheater and boiler, 32-liquefied ammonia feed-line.
The specific embodiment
Embodiment is referring to shown in Fig. 2-7, this liquid ammonia evaporator for denitrating flue gas, comprise Heat Room and be located at the stainless steel heat exchange tube in Heat Room, described Heat Room is comprised of bottom Heat Room 1 and top Heat Room 2, the top of bottom Heat Room 1 has denitration gas approach 3, the bottom of bottom Heat Room 1 has denitration exhanst gas outlet 4, and the bottom of top Heat Room 2 has hot-air inlets 5, and the top of top Heat Room 2 has hot air outlet 6.
Described stainless steel heat exchange tube comprises the heat exchanger tube 7 being located in bottom Heat Room 1 and is located at the revaporizer heat exchanger tube 11 in top Heat Room 2, and No. one time heat exchanger tube 7 is communicated with revaporizer heat exchanger tube 11, the tube wall of described revaporizer heat exchanger tube 11 is comprised of inwall 12 and outer wall 13, wherein inwall 12 is provided with equally distributed millimetre-sized aperture 14, and outer wall 13 is provided with equally distributed micron-sized micropore 15.
In the present embodiment, the entrance point of a heat exchanger tube 7 is again low head with the lower straighttube 8(that is positioned at the level of bottom Heat Room 1 bottom, for straight length forms) be communicated with, on lower straighttube 8, have be communicated with use with liquefied ammonia feed-line 32 liquefied ammonia import 9(according to the flow of liquefied ammonia, can there is one or several liquefied ammonia import, and the position of opening of liquefied ammonia import is generally lower straighttube maximum secting area place), the entrance point of revaporizer heat exchanger tube 11 is called again end socket with the upper straight tube 10(that is positioned at the level of top Heat Room 2 bottoms) be communicated with, upper straight tube 10 is communicated with the port of export of a heat exchanger tube 7 again, the port of export of revaporizer heat exchanger tube 11 is communicated with the revaporizer gathering tube 16 that is positioned at the level at top Heat Room 2 tops.Referring to Fig. 1, in the present embodiment, the caliber of lower straighttube 8 is 4～5 times of caliber of liquefied ammonia feed-line 32, and the caliber of upper straight tube 10 is liquefied ammonia carrier pipes, 6～8 times of 32 caliber.
In the present embodiment, a heat exchanger tube 7 is the snakelike tube fin type heat exchange pipe that many parallel interval arrange.The caliber of tube fin type heat exchange pipe is 15mm～25mm, and the fin height of tube fin type heat exchange pipe is caliber 50%～60%, and the spacing of fin is 2.5mm～3.5mm, and the spacing between tube fin type heat exchange pipe is 30mm～50mm.The interface of tube fin type heat exchange pipe and lower straighttube 8 is horizontal interface or vertical joint, and the center line of all tube fin type heat exchange pipes and the interface of lower straighttube 8 is in same level.Tube fin type heat exchange pipe is comprised of fin and heat exchanger tube, and the quantity of tube fin type heat exchange pipe can be determined according to liquefied ammonia evaporation capacity.
The length of described revaporizer heat exchanger tube and shape can be according to the spatial design of the disposal ability of evaporimeter and flue.Upper straight tube level when operation is installed, and the outlet of revaporizer heat exchanger tube is in the bottom of upper straight tube, and the import of revaporizer heat exchanger tube is uniform at the upper semi-circle column section of lower straighttube.In the present embodiment, revaporizer heat exchanger tube 11 includes the vertical tube that many parallel interval arrange.The thickness of the inwall 12 in vertical tube is 10 mm～15mm, and the aperture of the aperture 14 on inwall 12 is 1mm～3mm, and the aperture of the micropore 15 on outer wall 13 is 5um～10um.The percent opening of outer wall 13 is 1%～5%.The outer wall 13 of revaporizer heat exchanger tube consists of Stainless Steel Agglomeration Filter Core, and homodisperse micropore can make ammonia evenly discharge, and larger metal surface is also for the liquefied ammonia not evaporating completely provides larger heat exchange area.The inwall of revaporizer heat exchanger tube is comprised of 304 stainless steel perforates.
Whole flue-gas denitration process can, referring to Fig. 1, be provided with economizer 18 in the boiler 17 in Fig. 1.The catalyzed reactor 20 of exhaust gases passes of boiler tail and air preheater 24 minutes are for 30 3 sections of the exhaust gases passes 29 between exhaust gases passes 19, catalytic reactor and air preheater between boiler and catalytic reactor and the exhaust gases passes between air preheater and exhanst gas outlet.The air duct being communicated with boiler 17 by air preheater 24 minutes for 31 two sections of the air duct 23 between air intlet and air preheater and the air ducts between air preheater and boiler.Anticorrosion with traditional anticorrosion of flue duct measure of exhaust gases passes is identical.
Referring to Fig. 1, Fig. 2, the described liquefied ammonia vapo(u)rization system for denitrating flue gas, include liquid ammonia storage tank 28, liquid ammonia evaporator and ammonia-spraying grid 27, wherein liquid ammonia storage tank 2 is communicated with the stainless steel heat exchange tube in liquid ammonia evaporator by liquefied ammonia feed-line 32, in the exhaust gases passes 19 of ammonia-spraying grid 27 between boiler and catalytic reactor.Denitration gas approach 3 on liquid ammonia evaporator enters boiler channel 21 by flue gas and is communicated with the exhaust gases passes 29 between air preheater with catalytic reactor, denitration exhanst gas outlet 4 on liquid ammonia evaporator goes out boiler channel 22 by flue gas and is communicated with the exhaust gases passes 30 between exhanst gas outlet with air preheater, hot-air inlets 5 on liquid ammonia evaporator is communicated with the air duct 31 between boiler with air preheater by air branch road 25, and the hot air outlet 6 on liquid ammonia evaporator is communicated with ammonia-spraying grid 27 by mixed gas passage 26.
Referring to Fig. 1, Fig. 2, in the present embodiment, bottom Heat Room 1 is that exhaust gases passes in exhaust gases passes amplifies section, and top Heat Room 2 is that the air duct in air duct amplifies section, and exhaust gases passes amplifies section and air duct and amplifies and section at the upper cover place of fin-tube type heat exchanger, separate.
Technological process main in the present invention comprises: 1, the flue gas after denitration, through tube fin type heat exchange pipe and liquefied ammonia heat exchange, then enters exhaust gases passes and carries out follow-up desulfurization and dedusting processing.
2, air major part after air preheater enters boiler, and fraction is introduced top Heat Room 2 in liquid ammonia evaporator, evaporation and the ammonia, the liquefied ammonia that ooze out are carried out to heating and gasifying and dilution.
3, first liquefied ammonia be evaporated to ammonia through tube fin type heat exchange pipe by major part, ammonia enters revaporizer heat exchanger tube with the liquefied ammonia of carrying secretly, see through under pressure micropore and be diffused into top Heat Room, then carry out mixed diluting with hot-air (air entering from hot-air inlets, heated by air preheater) and become mist, unevaporated liquefied ammonia forms fine droplet on the surface of revaporizer heat exchanger tube (unevaporated liquefied ammonia appears micropore surface), be evaporated into ammonia and enter mist under hot air acting.The mist of above air and ammonia is through ammonia-spraying grid 27(ammonia nozzle) for denitrating flue gas, that is to say, ammonia in revaporizer heat exchanger tube and air fully mix with heat exchange after become mist and enter ammonia-spraying grid, then through ammonia-spraying grid, enter selective recall reduction reaction district again and carry out selective reduction denitration reaction.
In whole technical process, the flow of liquefied ammonia is major control object, determines the flow of liquefied ammonia according to the concentration of nitrogen oxides in effluent, flow, and in evaporimeter, the flow of high-temperature flue gas is that excessive assurance liquefied ammonia evaporates institute's calorific requirement, does not need strict control.The flow of hot-air is 20 times of left and right of the required ammonia flow of denitration, and the concentration of ammonia in gaseous mixture is controlled to 5% left and right.The ammonia not spreading out completely enters air ammonia mixing air channel by the road to be mixed with gaseous mixture.
In heat transfer process, described fin-tube type heat exchanger adopts the flue gas of high heating value to carry out heat exchange, that is to say tube fin type heat exchange pipe and flue gas cross-flow heat exchange, liquefied ammonia utilizes the flue gas of 300 ℃～400 ℃ to carry out evaporating after heat exchange, and the heat exchange amount of flue gas is 80%～100% of liquefied ammonia evaporation institute calorific requirement.Described revaporizer heat exchanger tube adopts the air after preheating to carry out heat exchange, that is to say, the ammonia being evaporated from fin-tube type heat exchanger and a small amount of liquefied ammonia discharge and heat exchange at revaporizer heat exchanger tube, revaporizer heat exchanger tube adopts the preheated air of 90 ℃～100 ℃ after air preheater heat exchange to carry out heat exchange and evaporation, in the Heat Room of top, ammonia mixes with preheated air, not completely the liquefied ammonia of evaporation in micropore and all can absorb heat on revaporizer heat exchanger tube surface and evaporate, the heat exchange amount of preheated air is 10%～30% of liquefied ammonia evaporation institute calorific requirement, can guarantee that the ammonia having gasified can again not liquefy in pipeline, the flow of preheated air is 10～20 times of ammonia amount.
Claims (10)
1. the liquid ammonia evaporator for denitrating flue gas, comprise Heat Room and be located at the stainless steel heat exchange tube in Heat Room, it is characterized in that: described Heat Room is comprised of bottom Heat Room (1) and top Heat Room (2), the top of bottom Heat Room (1) has denitration gas approach (3), the bottom of bottom Heat Room (1) has denitration exhanst gas outlet (4), the bottom of top Heat Room (2) has hot-air inlets (5), and the top of top Heat Room (2) has hot air outlet (6);
Described stainless steel heat exchange tube comprises the heat exchanger tube (7) being located in bottom Heat Room (1) and is located at the revaporizer heat exchanger tube (11) in top Heat Room (2), and a heat exchanger tube (7) is communicated with revaporizer heat exchanger tube (11), the tube wall of described revaporizer heat exchanger tube (11) is comprised of inwall (12) and outer wall (13), wherein inwall (12) is provided with equally distributed millimetre-sized aperture (14), and outer wall (13) is provided with equally distributed micron-sized micropore (15).
2. the liquid ammonia evaporator for denitrating flue gas according to claim 1, it is characterized in that: the entrance point of a described heat exchanger tube (7) is communicated with the lower straighttube (8) that is positioned at the level of bottom Heat Room (1) bottom, on lower straighttube (8), have the liquefied ammonia import (9) that is communicated with use with liquefied ammonia feed-line (32), the entrance point of described revaporizer heat exchanger tube (11) is communicated with the upper straight tube (10) that is positioned at the level of top Heat Room (2) bottom, upper straight tube (10) is communicated with the port of export of a heat exchanger tube (7) again, the port of export of revaporizer heat exchanger tube (11) is communicated with the revaporizer gathering tube (16) that is positioned at the level at top Heat Room (2) top.
3. the liquid ammonia evaporator for denitrating flue gas according to claim 2, it is characterized in that: the caliber of described lower straighttube (8) is 4～5 times of caliber of liquefied ammonia feed-line (32), the caliber of upper straight tube (10) is 6～8 times of caliber of liquefied ammonia feed-line (32).
4. the liquid ammonia evaporator for denitrating flue gas according to claim 2, is characterized in that: a described heat exchanger tube (7) is snakelike tube fin type heat exchange pipe.
5. the liquid ammonia evaporator for denitrating flue gas according to claim 4, it is characterized in that: the caliber of described tube fin type heat exchange pipe is 15mm～25mm, the fin height of tube fin type heat exchange pipe is 50%～60% of caliber, the spacing of fin is 2.5mm～3.5mm, and the spacing between tube fin type heat exchange pipe is 30mm～50mm.
6. the liquid ammonia evaporator for denitrating flue gas according to claim 4, it is characterized in that: the interface of described tube fin type heat exchange pipe and lower straighttube (8) is horizontal interface or vertical joint, the center line of the interface of all tube fin type heat exchange pipes and lower straighttube (8) is in same level.
7. the liquid ammonia evaporator for denitrating flue gas according to claim 2, is characterized in that: the vertical tube that described revaporizer heat exchanger tube (11) arranges for many parallel interval.
8. the liquid ammonia evaporator for denitrating flue gas according to claim 7, it is characterized in that: the thickness of the inwall in described vertical tube (12) is 10 mm～15mm, the aperture of the aperture (14) on inwall (12) is 1mm～3mm, and the aperture of the micropore (15) on outer wall (13) is 5um～10um.
9. the liquid ammonia evaporator for denitrating flue gas according to claim 7, is characterized in that: the percent opening of described outer wall (13) is 1%～5%.
10. the liquefied ammonia vapo(u)rization system for denitrating flue gas, include liquid ammonia storage tank (28), liquid ammonia evaporator and ammonia-spraying grid (27), wherein liquid ammonia evaporator comprises Heat Room and is located at the stainless steel heat exchange tube in Heat Room, liquid ammonia storage tank (28) is communicated with the stainless steel heat exchange tube in liquid ammonia evaporator by liquefied ammonia feed-line (32), in the exhaust gases passes (19) of ammonia-spraying grid (27) between boiler and catalytic reactor, it is characterized in that: described liquid ammonia evaporator is the liquid ammonia evaporator for denitrating flue gas described in any one in the claims 1-9, denitration gas approach (3) on liquid ammonia evaporator enters boiler channel (21) by flue gas and is communicated with the exhaust gases passes (29) between air preheater with catalytic reactor, denitration exhanst gas outlet (4) on liquid ammonia evaporator goes out boiler channel (22) by flue gas and is communicated with the exhaust gases passes (30) between exhanst gas outlet with air preheater, hot-air inlets on liquid ammonia evaporator (5) is communicated with the air duct (31) between boiler with air preheater by air branch road (25), hot air outlet on liquid ammonia evaporator (6) is communicated with ammonia-spraying grid (27) by mixed gas passage (26).
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| CN201210249329.2A CN102743889B (en) | 2012-07-19 | 2012-07-19 | Liquid ammonia evaporator and liquid ammonia evaporation system for flue gas denitration |
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| CN201210249329.2A CN102743889B (en) | 2012-07-19 | 2012-07-19 | Liquid ammonia evaporator and liquid ammonia evaporation system for flue gas denitration |
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| CN109163216B (en) * | 2018-09-26 | 2024-02-09 | 苏州市创优净化科技有限公司 | Safe intelligent liquid ammonia vaporization system |
| CN110180357B (en) * | 2019-06-11 | 2021-12-14 | 淮南聚生化工科技有限公司 | Liquid ammonia evaporator for flue gas denitration |
| CN111744222A (en) * | 2020-06-23 | 2020-10-09 | 莫清翔 | Liquid ammonia evaporator for flue gas denitration |
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| 孙克勤,沈凯等.SCR烟气脱硝液氨系统关键设备的仿真.《中国环境科学学会学术年会论文集》.2010,全文. * |
| 张治忠.台山电厂5号机组烟气脱硝液氨储存区设计.《电力环境保护》.2008,第24卷(第1期),全文. |
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