CN109876626A - A kind of three-stage urea pyrolysis ammonia denitrating system and its working method - Google Patents
A kind of three-stage urea pyrolysis ammonia denitrating system and its working method Download PDFInfo
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- CN109876626A CN109876626A CN201910150905.XA CN201910150905A CN109876626A CN 109876626 A CN109876626 A CN 109876626A CN 201910150905 A CN201910150905 A CN 201910150905A CN 109876626 A CN109876626 A CN 109876626A
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 71
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 239000004202 carbamide Substances 0.000 title claims abstract description 60
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 48
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims abstract description 27
- 239000000243 solution Substances 0.000 claims abstract description 96
- 239000007788 liquid Substances 0.000 claims abstract description 32
- 239000000815 hypotonic solution Substances 0.000 claims abstract description 18
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000003546 flue gas Substances 0.000 claims abstract description 16
- 239000012895 dilution Substances 0.000 claims abstract description 14
- 238000010790 dilution Methods 0.000 claims abstract description 14
- 239000002994 raw material Substances 0.000 claims abstract description 14
- 230000001105 regulatory effect Effects 0.000 claims abstract description 12
- 238000004090 dissolution Methods 0.000 claims abstract description 5
- 238000010438 heat treatment Methods 0.000 claims abstract description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 14
- 239000002904 solvent Substances 0.000 claims description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 8
- 238000000354 decomposition reaction Methods 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 239000001569 carbon dioxide Substances 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- 239000000126 substance Substances 0.000 claims description 2
- 230000003139 buffering effect Effects 0.000 claims 1
- 238000002485 combustion reaction Methods 0.000 claims 1
- 239000004744 fabric Substances 0.000 claims 1
- 238000010248 power generation Methods 0.000 abstract description 2
- 230000000903 blocking effect Effects 0.000 abstract 1
- 238000001321 HNCO Methods 0.000 description 4
- OWIKHYCFFJSOEH-UHFFFAOYSA-N Isocyanic acid Chemical compound N=C=O OWIKHYCFFJSOEH-UHFFFAOYSA-N 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- 239000000908 ammonium hydroxide Substances 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 206010000372 Accident at work Diseases 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Classifications
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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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- Treating Waste Gases (AREA)
Abstract
The present invention relates to a kind of three-stage urea pyrolysis ammonia denitrating system and its working methods, belong to power generation field.Although urea pyrolysis Ammonia Process security performance is high, there are operating costs high, easy the problems such as blocking.System is mainly made of equipment such as raw material cabin, screw feeder, solution preparing device, solution transfer pump hypotonic solution preheater, solution surge tank, booster, recycle valve, high-pressure solution regulating valve, flowmeter, high-pressure solution heater, pyrolysis reactor, dilution mixer, blowers.It is compared with other methods, urea pyrolysis process is divided into three sections of concatenated processes by the present invention, it may be assumed that urea dissolution preheating, high-pressure solution heating, urea liquid thoroughly decompose.Due to high-temperature flue gas heat source mediate contact, have that operating cost is low, effectively avoids the technical characterstics such as system jams.
Description
Technical field
The present invention relates to a kind of urea pyrolysis ammonia denitrating systems, belong to power generation field.
Background technique
Large-scale power station coal-burning boiler be more than 90% all select the selective-catalytic-reduction denitrified technique of SCR, for removing in flue gas
NOx.Denitrification reducing agent generally selects liquefied ammonia, ammonium hydroxide or urea.Liquefied ammonia and ammonium hydroxide have toxicity, corrosivity and explosion hazard,
Belong to major hazard source, bigger security risk is brought to actual production process.In contrast, urea due to it is nontoxic,
The advantages that using conveniently, safely storing and transporting, Rapid Popularization gradually is obtained in the SCR denitration engineering of many coal-burning power plants and is answered
With such as application No. is the Chinese patents of 201811380706.X.
Currently, urea pyrolysis Ammonia Process is most of all to have Adiabatic Decomposition room, being burnt using diesel/natural gas, it is high to generate
Warm flue gas or by electrically heated high temperature air as heat source, directly contact with urea liquid be allowed to decomposition generation be diluted
Ammonia, Benitration reactor is then sent by ammonia-spraying grid.
But the technology there are operating costs the problems such as high, Adiabatic Decomposition room easily blocks, affect the economy of production system
Property and reliability.For example, for providing the system of heat source, the unit annual operation of 1 600MW grade using fuel oil or combustion gas
Expense is more than 4,000,000 yuan；System using electric heating air as heat source, the unit annual operating cost of identical capacity is about
1500000 yuan.In addition, the factors such as Adiabatic Decomposition room temperature is relatively low, nozzle atomization effect is poor, flue gas or air oil-containing dust-laden, all may be used
It can will lead to and quickly form crystallization deposition object in a short time, block Adiabatic Decomposition room, cause industrial accident.
Summary of the invention
It is an object of the invention to overcome the above deficiencies in the existing technologies, a kind of three-stage urea pyrolysis system is provided
Ammonia denitrating system and its working method.It is low with operating cost, effective to avoid crystallization heavy compared with current urea pyrolysis technique
The high technological merit of the formation of product object, operational reliability.
Technical solution used by the present invention solves the above problems is: a kind of three-stage urea pyrolysis ammonia denitrating system,
It is characterised in that it includes boiler, Benitration reactor and air preheater, the boiler pass sequentially through horizontal flue, reversal chamber and
Vertical ascent flue is connected to Benitration reactor, and Benitration reactor is connected to air preheater, arrangement in the horizontal flue
There are high temperature superheater and high temperature reheater, the reversal chamber arranged beneath has economizer hopper.
Three-stage urea pyrolysis ammonia denitrating system further includes raw material cabin, screw feeder, solution preparing device, solution conveying
Pump, hypotonic solution preheater, solution surge tank, booster, flowmeter, high-pressure solution heater, pyrolysis reactor, dilution mixing
Device and blower；The raw material cabin, screw feeder, solution preparing device and solution transfer pump are sequentially connected, and solution preparing device
Solvent control valve is installed, the hypotonic solution preheater is arranged between Benitration reactor and air preheater in solvent conduit
Flue in, and the entrance and exit of hypotonic solution preheater is connect with the outlet of solution transfer pump and solution surge tank respectively,
The solution surge tank is also connected to the entrance of booster, and the export pipeline of booster is divided into two-way, passes through recycling all the way
Valve is connected to the export pipeline of hypotonic solution preheater, and another way passes sequentially through high-pressure solution regulating valve and flowmeter and high pressure solution
The entrance pipe of liquid heater is connected to, and the high-pressure solution heater is arranged in horizontal flue, and high-pressure solution heater position
Region between high temperature superheater and high temperature reheater, the outlet of the high-pressure solution heater and the entrance of pyrolysis reactor
Connection, the pyrolysis reactor is arranged in reversal chamber, the outlet of the pyrolysis reactor and the outlet of blower respectively with dilution
The outlet of mixer connection, the dilution mixer is connected to the vertical ascent flue before Benitration reactor.
Above-mentioned three-stage urea pyrolysis ammonia denitrating system, working method is: the urea raw material being stored in raw material cabin,
Solution preparing device is sent by screw feeder and is divided with the mutual mixed dissolution of water phase, the quality of generation urea liquid, urea liquid
Number, i.e. water flow, are controlled by solvent control valve.Later, urea liquid is sent into hypotonic solution preheater by solution transfer pump
It is tentatively heated up, prevents urea liquid from recrystallizing.Urea liquid after preliminary heating is transported to the storage of solution surge tank, so
Afterwards after booster improves pressure head, it is divided into two parts, a part comes back to solution surge tank after recycle valve, another
Part then successively after high-pressure solution regulating valve and flowmeter, is sent into high-pressure solution heater and is thoroughly heated, to reach
Close to the temperature of urea liquid fast decoupled.
For the pyrolysis urea liquid flow of denitrating system, measures by flowmeter and controlled by high-pressure solution regulating valve.
On the one hand solution surge tank provides stable urea liquid source for booster, on the other hand cooperate recycle valve and high-pressure solution
Regulating valve for accurately controlling the urea liquid flow into high-pressure solution heater, while playing solution storage and pressure
Buffer function.The urea solution temperature of high-pressure solution heater outlet is then fed to heat very close to its fast decoupled temperature
It solves reactor and carries out heat temperature raising, thoroughly carry out the reaction of pyrolytic process, generate ammonia and carbon dioxide, including following two master
It reacts:
CO(NH2)2 → HNCO + NH3
HNCO + H2O → CO2 + NH3
High-pressure solution heater and pyrolysis reactor are all arranged using with flow of flue gas direction concurrent, to reduce high temperature side
Tube wall temperature.Compared with high-pressure solution heater, pyrolysis reactor is arranged in the relatively low steering chamber region of flue-gas temperature, has
Conducive to the tube wall temperature for reducing pyrolysis reactor, device security is improved.The ammonia and carbon dioxide flowed out from pyrolysis reactor
Into dilution mixer, the air being sent into blower is mixed, and is on the one hand reduced the concentration of ammonia, is made it below the explosion of ammonia
On the other hand lower limit suitably reduces the temperature of ammonia.The mixed gas of the ammonia and air that flow out from dilution mixer, is admitted to
Vertical ascent flue before Benitration reactor is mixed with the flue gas after the preliminary ash disposal of economizer hopper, finally jointly into
Enter denitration reactor inlet and carries out removing NOx reaction.
Urea pyrolysis process is divided into three Duan Liucheng by the present invention, it may be assumed that the pre- hot preparation chemical property of urea material dissolution is stablized
Hypotonic solution, high-pressure solution is heated to fast decoupled temperature, urea liquid thoroughly decomposition prepares ammonia.Due to eliminating tradition
Adiabatic Decomposition room in urea pyrolysis technique, and using boiler itself flue gas heat as the power heat source of urea pyrolysis, no
Need to significantly reduce the initial outlay and operating cost of the system using diesel oil, natural gas or electric energy.In addition, with tradition
In technique, for urea liquid compared with high-temperature flue gas or high temperature air directly contact the mode being pyrolyzed, the present invention is hot by urea
Solution preocess is divided into three concatenated mediate contact processes, has fundamentally prevented the formation for crystallizing deposit, can effectively avoid
The problem of system jams.
Detailed description of the invention
Fig. 1 is the system structure diagram of the embodiment of the present invention.
In figure: 1- boiler, 2- high temperature superheater, 3- high-pressure solution heater, 4- high temperature reheater, 5- pyrolysis reactor,
6- dilutes mixer, and 7- blower, 8- vertical ascent flue, 9- flowmeter, 10- high-pressure solution regulating valve, 11- booster, 12- is again
Circulating valve, 13- solution surge tank, 14- Benitration reactor, 15- hypotonic solution preheater, 16- raw material cabin, 17- screw feeder,
18- solution preparing device, 19- solvent control valve, 20- solution transfer pump, 21- air preheater, 22- economizer hopper, 23- are turned to
Room, 24- horizontal flue.
Specific embodiment
The present invention is described in further detail with reference to the accompanying drawing and by embodiment, and following embodiment is to this hair
Bright explanation and the invention is not limited to following embodiments.
Embodiment.
Referring to Fig. 1, three-stage urea pyrolysis ammonia denitrating system in the present embodiment, including boiler 1, Benitration reactor 14
With air preheater 21, the boiler 1 passes sequentially through horizontal flue 24, reversal chamber 23 and vertical ascent flue 8 and denitration reaction
Device 14 is connected to, and Benitration reactor 14 is connected to air preheater 21, and 2 He of high temperature superheater is disposed in the horizontal flue 24
High temperature reheater 4,23 arranged beneath of reversal chamber have economizer hopper 22.
Three-stage urea pyrolysis ammonia denitrating system further includes raw material cabin 16, screw feeder 17, solution preparing device 18, molten
Liquid delivery pump 20, hypotonic solution preheater 15, solution surge tank 13, booster 11, flowmeter 9, high-pressure solution heater 3, heat
Solve reactor 5, dilution mixer 6 and blower 7；The raw material cabin 16, screw feeder 17, solution preparing device 18 and solution conveying
Pump 20 is sequentially connected, and solvent control valve 19 is equipped in the solvent conduit of solution preparing device 18, the hypotonic solution preheater
15 are arranged in the flue between Benitration reactor 14 and air preheater 21, and the entrance and exit of hypotonic solution preheater 15
It is connect respectively with the outlet of solution transfer pump 20 and solution surge tank 13, entrance of the solution surge tank 13 also with booster 11
Connection, and the export pipeline of booster 11 is divided into two-way, passes through the outlet of recycle valve 12 and hypotonic solution preheater 15 all the way
Pipeline connection, another way passes sequentially through high-pressure solution regulating valve 10 and flowmeter 9 and the entrance pipe of high-pressure solution heater 3 connects
Logical, the high-pressure solution heater 3 is arranged in horizontal flue 24, and high-pressure solution heater 3 is located at high temperature superheater 2 and height
The outlet in the region between warm reheater 4, the high-pressure solution heater 3 is connected to the entrance of pyrolysis reactor 5, the pyrolysis
Reactor 5 is arranged in reversal chamber 23, and the outlet of the pyrolysis reactor 5 and the outlet of blower 7 connect with dilution mixer 6 respectively
Logical, the outlet of the dilution mixer 6 is connected to the vertical ascent flue 8 before Benitration reactor 14.
The working method of the system is: the urea raw material being stored in raw material cabin 16 is sent into molten by screw feeder 17
Liquid preparing device 18 and the mutual mixed dissolution of water phase, generate the urea liquid that mass fraction is 50%, water flow required for process, by
Solvent control valve 19 is controlled.Later, urea liquid is sent into hypotonic solution preheater 15 by solution transfer pump 20 and is carried out tentatively
50 DEG C are warming up to, prevents urea liquid from recrystallizing.Urea liquid after preliminary heating is transported to the storage of solution surge tank 13, so
Afterwards after booster 11 improves solution pressure to 15kPa, it is divided into two parts, a part comes back to after recycle valve 12
Solution surge tank 13, another part then successively after high-pressure solution regulating valve 10 and flowmeter 9, are sent into high-pressure solution heater
3 carry out thoroughly being heated to 130 DEG C, to reach the temperature close to urea liquid fast decoupled.
For the pyrolysis urea liquid flow of denitrating system, measures by flowmeter 9 and controlled by high-pressure solution regulating valve 10
System.13 one side of solution surge tank is that booster 11 provides stable urea liquid source, on the other hand cooperates recycle valve 12
With high-pressure solution regulating valve 10, for accurately controlling the urea liquid flow into high-pressure solution heater 3, while playing molten
Liquid storage and pressure buffer effect.The urea liquid that high-pressure solution heater 3 exports enters pyrolysis reactor 5 and carries out heating liter
Temperature thoroughly carries out the reaction of pyrolytic process, generates ammonia and carbon dioxide, including following two key reaction:
CO(NH2)2 → HNCO + NH3
HNCO + H2O → CO2 + NH3
High-pressure solution heater 3 and pyrolysis reactor 5 are all arranged using with flow of flue gas direction concurrent, to reduce high temperature side
Tube wall temperature.Compared with high-pressure solution heater 3, pyrolysis reactor 5 is arranged in the relatively low reversal chamber 23 of flue-gas temperature
Region advantageously reduces the tube wall temperature of pyrolysis reactor, improves device security.From pyrolysis reactor 5 flow out ammonia and
Carbon dioxide enters dilution mixer 6, and the air being sent into blower 7 mixes, and so that ammonia concentration is down to 5%, mixed gas temperature
It is down to 340 DEG C.The mixed gas of the ammonia and air that are flowed out from dilution mixer 6, hanging down before being admitted to Benitration reactor 14
Straight uptake flue 8, mixes with the flue gas after the preliminary ash disposal of economizer hopper 22, and the last Benitration reactor 14 that enters jointly enters
Mouth carries out removing NOx reaction.
It is any to be familiar with although the present invention is disclosed as above with embodiment, its protection scope being not intended to limit the invention
The technical staff of this technology changes and retouches made without departing from the spirit and scope of the invention, should belong to this hair
Bright protection scope.
Claims (5)
1. a kind of three-stage urea pyrolysis ammonia denitrating system, which is characterized in that including boiler (1), Benitration reactor (14) and
Air preheater (21), the boiler (1) pass sequentially through horizontal flue (24), reversal chamber (23) and vertical ascent flue (8) with
Benitration reactor (14) connection, and Benitration reactor (14) is connected to air preheater (21), the interior cloth of the horizontal flue (24)
It is equipped with high temperature superheater (2) and high temperature reheater (4), reversal chamber (23) arranged beneath there are economizer hopper (22)；It is special
Sign is, further includes raw material cabin (16), screw feeder (17), solution preparing device (18), solution transfer pump (20), hypotonic solution
Preheater (15), solution surge tank (13), booster (11), flowmeter (9), high-pressure solution heater (3), pyrolysis reactor
(5), mixer (6) and blower (7) are diluted；The raw material cabin (16), screw feeder (17), solution preparing device (18) and solution
Delivery pump (20) is sequentially connected, and solvent control valve (19), the low pressure are equipped in the solvent conduit of solution preparing device (18)
Solution preheater (15) is arranged in the flue between Benitration reactor (14) and air preheater (21), and hypotonic solution preheats
The entrance and exit of device (15) is connect with the outlet of solution transfer pump (20) and solution surge tank (13) respectively, the solution buffering
Tank (13) is also connected to the entrance of booster (11), and the export pipeline of booster (11) is divided into two-way, passes through recycling all the way
Valve (12) is connected to the export pipeline of hypotonic solution preheater (15), and another way passes sequentially through high-pressure solution regulating valve (10) and stream
Meter (9) is connected to the entrance pipe of high-pressure solution heater (3), and the outlet and pyrolysis of the high-pressure solution heater (3) are anti-
The entrance of device (5) is answered to be connected to, the outlet of the pyrolysis reactor (5) and the outlet of blower (7) connect with dilution mixer (6) respectively
Logical, the outlet of dilution mixer (6) is connected to the vertical ascent flue (8) before Benitration reactor (14).
2. three-stage urea pyrolysis ammonia denitrating system according to claim 1, which is characterized in that the high-pressure solution adds
Hot device (3) is arranged in horizontal flue (24), and high-pressure solution heater (3) is located at high temperature superheater (2) and high temperature reheater
(4) between, the pyrolysis reactor (5) is arranged in reversal chamber (23).
3. a kind of working method of three-stage urea pyrolysis ammonia denitrating system as claimed in claim 1 or 2, feature exist
In, urea raw material in raw material cabin (16) by screw feeder (17) be sent into solution preparing device (18) and and water be mutually mixed it is molten
Solution, forms urea liquid, and the mass fraction of urea liquid is controlled by solvent control valve (19)；Urea liquid passes through solution transfer pump
(20) hypotonic solution preheater (15) are sent into tentatively to be heated up, are transported to storage in solution surge tank (13) later, pass through
After booster (11) improves pressure head, it is divided into two parts, a part comes back to solution surge tank after recycle valve (12)
(13) in, another part then passes through high-pressure solution regulating valve (10) and flowmeter (9), be admitted to high-pressure solution heater (3) into
Row heating, last urea liquid are admitted to pyrolysis reactor (5), thoroughly carry out pyrolytic reaction and generate ammonia and carbon dioxide；Ammonia
Gas and carbon dioxide enter dilution mixer (6), and the air being sent into blower (7) mixes, and enter Benitration reactor later
(14) the vertical ascent flue (8) before, with flue gas be mixed and fed into Benitration reactor (14) carry out removing NOx react.
4. the working method of three-stage urea pyrolysis ammonia denitrating system according to claim 3, which is characterized in that urea
Pyrolytic process is divided into three sections of concatenated processes, comprising: the stable hypotonic solution of the pre- hot preparation chemical property of urea material dissolution, height
Pressure solution liquid is heated to fast decoupled temperature, urea liquid, and thoroughly decomposition prepares ammonia；The heat source of all processes is boiler (1) combustion
The flue gas generated is burnt, and uses mediate contact mode with the contact of flue gas heat source.
5. the working method of three-stage urea pyrolysis ammonia denitrating system according to claim 3, which is characterized in that high pressure
Solution heater (3) and pyrolysis reactor (5) all using with arranged by the way of the fair current of flow of flue gas direction.
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| CN111963283A (en) * | 2020-08-11 | 2020-11-20 | 航天环境工程有限公司 | Novel urea hydrolysis system with product gas treatment device and application |
| CN114876613A (en) * | 2022-05-24 | 2022-08-09 | 安庆船用电器有限责任公司 | Marine urea supply injection apparatus |
| CN115159544A (en) * | 2022-06-07 | 2022-10-11 | 华能太原东山燃机热电有限责任公司 | A pyrolysis type denitrification device for preventing urea crystallization |
| CN118253182A (en) * | 2024-05-11 | 2024-06-28 | 北京华能长江环保科技研究院有限公司 | A high-efficiency denitrification agent waterless injection ammonia production system and method |
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