CN106705091B - A kind of system and method for slowing down SCR catalyst inactivation and air preheater and blocking - Google Patents
A kind of system and method for slowing down SCR catalyst inactivation and air preheater and blocking Download PDFInfo
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- CN106705091B CN106705091B CN201611192800.3A CN201611192800A CN106705091B CN 106705091 B CN106705091 B CN 106705091B CN 201611192800 A CN201611192800 A CN 201611192800A CN 106705091 B CN106705091 B CN 106705091B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/006—Layout of treatment plant
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8628—Processes characterised by a specific catalyst
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8631—Processes characterised by a specific device
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/88—Handling or mounting catalysts
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L15/00—Heating of air supplied for combustion
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/10—Nitrogen; Compounds thereof
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/10—Nitrogen; Compounds thereof
- F23J2215/101—Nitrous oxide (N2O)
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/20—Sulfur; Compounds thereof
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2219/00—Treatment devices
- F23J2219/10—Catalytic reduction devices
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
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- Engineering & Computer Science (AREA)
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- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Biomedical Technology (AREA)
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- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
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- General Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Treating Waste Gases (AREA)
Abstract
Conventional boiler tail portion equipment method for arranging has been carried out following improvement by a kind of system and method for slowing down SCR catalyst inactivation and air preheater and blocking, system：Air preheater is divided into two sections, and flue gas flows successively through economizer, high-temperature air preheater, electrostatic precipitator, SCR device, low-temperature air preheater, steam air heater, low cold precipitator, and desulfurizing tower is finally discharged into air from chimney；Smoke temperature at SCR device is about 200 DEG C, reducing agent needed for denitration is produced using ureal antigen, in dissolving tank simultaneously dissolved urea and ammonium nitrate, mixed solution generates ammonia by heating, hydrolysis and nitric acid gas sprays into SCR device together, realizes that the highly effective and safe of SCR under low temperature is run by a kind of new NO reduction reactions：HNO3+2NO+3NH3→3N2+5H2O, the reaction is in 200 DEG C of NO reduction rates up to 90%；The present invention can slow down the blocking of the inactivation and air preheater of SCR catalyst while ensureing boiler tail denitration efficiency, improve economy and the safety of boiler operatiopn.
Description
Technical field
The invention belongs to coal-fired field of thermal power, more particularly to one kind slowing down SCR catalyst inactivation and air preheater
The system and method for blocking.
Background technology
SCR device is often arranged in boiler tail system to reach NO in removing flue gasxPurpose, traditional denitration reaction
Catalyst optimum working temperature is 320 DEG C -420 DEG C, so SCR denitration device is typically located at economizer exit and air preheat
Between device entrance, be arranged so one the disadvantage is that the flying dust in flue gas can cause catalyst abrasion, block and chemical poisoning,
The efficiency for greatly reducing SCR denitration reaction, leads to NOxDischarge capacity it is exceeded.
In addition, the spray ammonia for failing to denitration reaction in SCR will escape into the air preheater in downstream, and and SO3, water steam
Gas, which reacts, generates ammonium hydrogen sulfate (ABS), and ABS is adhered to air preheater and adsorbs the flying dust in flue gas, and it is stifled that dust stratification occurs
Fill in phenomenon.Air preheater blocks the efficiency for seriously affecting boiler, increases flue gas collateral resistance, and power plant fans power consumption is caused to increase,
Greatly reduce the economy of power plants generating electricity.
Invention content
The purpose of the present invention is to provide one kind capable of preventing catalyst inactivation, while slowing down air preheater blocking, from
And improve the economy of system operation and the boiler tail equipment for slowing down catalyst inactivation and air preheater blocking of safety
Arrangement system and method.
In order to achieve the above objectives, system of the invention include for tail flue gas exchange heat and purify flow of flue gas system and
The reducing agent supply system of reducing agent is provided for SCR denitration reaction；
The flow of flue gas system includes connecting the economizer of boiler low-temperature superheater outlet flue gas, the flue gas of economizer
Outlet is connect with high-temperature air preheater, and the exhanst gas outlet of high-temperature air preheater is connect with electrostatic precipitator, electrostatic precipitator
Outlet is connect with SCR denitration device, and SCR denitration device outlet is connect with low-temperature air preheater, the cigarette of low-temperature air preheater
Gas outlet is connect with steam air heater, and steam air heater outlet is connect with cold precipitator, and cold precipitator outlet is connect with desulfurizing tower, desulfurization
Tower outlet is connect with chimney；
The reducing agent supply system includes the dissolving tank for connecting urea conveyer and nitric acid/ammonium nitrate conveyer, molten
The outlet of solution slot is connect through solution force (forcing) pump with solution storage slot, and the outlet of solution storage slot connects through solution transfer pump and hydrolysis heat exchanger
It connects, hydrolysis heat exchanger exit is connect with the entrance of solution hydrolyzer, and the outlet of solution hydrolyzer is connect with SCR denitration device.
Pressure fan is also associated on the steam air heater, steam air heater air outlet slit is connect with low-temperature air preheater, low temperature
The air outlet slit of air preheater is connect with high-temperature air preheater, and the outlet of high-temperature air preheater is connected to burner hearth.
The solution hydrolyzer is equipped with steam inlet connection turbine low pressure cylinder pumping, the raffinate outlet of solution hydrolyzer
It is connect with hydrolysis heat exchanger, the raffinate outlet for hydrolyzing heat exchanger divides two-way, is connect all the way with dissolving tank, another way discharge is extra residual
Liquid.
The present invention slows down the method that SCR catalyst inactivation and air preheater block, and includes the following steps：
Boiler low-temperature superheater outlet flue gas passes sequentially through economizer first and high-temperature air preheater exchanges heat, high temperature
The flue gas exit temperature of air preheater is about 200 DEG C, and subsequent flue gas enters electrostatic precipitator and removes coal ash particle and big portion
Coal ash dust, the flue gas after dust removal process is divided to enter SCR denitration device, the NO in SCR denitration device in flue gas is injected into
Ammonia and nitric acid gas restored, the exiting flue gas of SCR denitration device passes sequentially through low-temperature air preheater and warm wind again
One Secondary Air of device heating boiler, it is about 80 DEG C that steam air heater, which exports smoke temperature, is subsequently entered thin in cold precipitator removing flue gas
Dust particle, the flue gas after too low low temperature dedusting enter back into the SO in desulfurizing tower removing flue gas2, last flue gas is via chimney
It is discharged into air；
Urea conveyer and nitric acid/ammonium nitrate conveyer are transported to urea and nitric acid or ammonium nitrate in dissolving tank pass through respectively
Wiring solution-forming is stirred, the mixed solution of urea, nitric acid or ammonium nitrate is then transported to solution storage slot using solution force (forcing) pump
In be forced into pressure 2.6MPa, being then transported to the raffinate that hydrolysis heat exchanger and solution hydrolyzer come out by solution transfer pump exchanges heat,
The mixed solution of hydrolysis heat exchanger exit is heated to about 180 DEG C, and nitric acid or decomposing ammonium nitrate are NH at this time3And HNO3, then mixed
Close solution and be transported to solution hydrolyzer, by the steam that turbine low pressure cylinder extracts be passed through the cylinder bottom of solution hydrolyzer directly with it is molten
The hydrolysis that liquid mixing carries out urea generates NH3, then the NH that is generated with nitric acid before or decomposing ammonium nitrate3And HNO3It sprays together
Enter and denitration reaction occurs in SCR denitration device.
The molar ratio of the urea and ammonium nitrate is 1:1.
The molar ratio of the urea and nitric acid is 1.5:1.
About 200 DEG C of Residue temperature being discharged from solution hydrolyzer bottom is introduced into hydrolysis heat exchanger heating mixed solution, water
The Residue temperature of solution heat exchanger exit is down to 90 DEG C or so and enters dissolving tank, and extra raffinate is sent to sewage plant processing.
The denitration reaction occurred in the SCR denitration equipment is：HNO3+2NO+3NH3→3N2+5H2O, the reaction exist
Denitration efficiency at 200 DEG C is up to 90%.
The air is conveyed by pressure fan, passes sequentially through steam air heater, low-temperature air preheater, high-temperature air preheater,
Primary and secondary air after heat absorption heating as coal dust firing is sent into burner hearth.
The present invention uses HNO in SCR device3+2NO+3NH3→3N2+5H2The efficient reduction of NO under a kind of this low temperature of O
It reacts to replace traditional SCR denitration to react, makes SCR device that can pacify at 200 DEG C by the way that ammonium nitrate is added in reducing agent
Full Effec-tive Function improves the arrangement of boiler tail devices in system, has the following advantages that based on this：
Cleaner is arranged before SCR device, slows down flying dust to the abrasion blocking of SCR catalyst and chemical poisoning,
Greatly alleviate the inactivation of catalyst；
Air preheater is divided into two sections of arrangements, high temperature section is arranged in before SCR, is avoided ABS and is made to high temperature air preheater
At blocking, and SCR is run at 200 DEG C or so, and catalyst is to SO2Oxidation effectiveness it is very weak, so also slowing down low temperature significantly
The blocking of air preheat；
Reducing agent ammonia needed for denitration is prepared using traditional ureal antigen, can complete to add while ammonium nitrate
Enter, without additionally increasing other equipment.
Description of the drawings
Fig. 1 is the structure principle chart of the present invention.
In figure：1 is economizer, and 2 be high-temperature air preheater, and 3 be electrostatic precipitator, and 4 be SCR denitration device, and 5 be low temperature
Air preheater, 6 be steam air heater, and 7 be cold precipitator, and 8 be desulfurizing tower, and 9 be chimney, and 10 be urea conveyer, 11 for nitric acid/
Ammonium nitrate conveyer, 12 be dissolving tank, and 13 be solution force (forcing) pump, and 14 be solution storage slot, and 15 be solution transfer pump, and 16 be hydrolysis
Heat exchanger, 17 be solution hydrolyzer, and 18 be pressure fan.
Specific implementation mode
Below in conjunction with attached drawing, the present invention is described in further detail.
As shown in Figure 1, the present invention system, include for tail flue gas exchange heat and purify flow of flue gas system and be
SCR denitration reaction provides the reducing agent supply system of reducing agent.
Flow of flue gas system includes economizer 1, high-temperature air preheater 2, electrostatic precipitator 3, SCR denitration device 4, low temperature
Air preheater 5, steam air heater 6, cold precipitator 7, desulfurizing tower 8 and chimney 9.Wherein, boiler low-temperature superheater exhanst gas outlet connects
1 smoke inlet of economizer is connect, 1 exhanst gas outlet of economizer connects 2 smoke inlet of high-temperature air preheater, high-temperature air preheater 2
Exhanst gas outlet connects 3 smoke inlet of electrostatic precipitator, and 3 exhanst gas outlet of electrostatic precipitator connects 4 smoke inlet of SCR denitration device,
4 exhanst gas outlet of SCR denitration device connects 5 smoke inlet of low-temperature air preheater, and the connection of 5 exhanst gas outlet of low-temperature air preheater is warm
6 smoke inlet of wind device, the outlet of steam air heater flue gas 6 connection 7 smoke inlet of cold precipitator, the connection of 7 exhanst gas outlet of cold precipitator
8 smoke inlet of desulfurizing tower, 8 exhanst gas outlet of desulfurizing tower connect chimney 9；Pressure fan 18 is also associated on steam air heater 6, steam air heater 6 is empty
Gas outlet is connect with low-temperature air preheater 5, and the air outlet slit of low-temperature air preheater 5 is connect with high-temperature air preheater 2, high
The outlet of warm air preheater 2 is connected to burner hearth.
Reducing agent supply system includes urea conveyer 10, nitric acid/ammonium nitrate conveyer 11, dissolving tank 12, solution pressurization
Pump 13, solution storage slot 14, solution transfer pump 15, hydrolysis heat exchanger 16 and solution hydrolyzer 17.Wherein, 10 He of urea conveyer
Nitric acid/ammonium nitrate conveyer 11 connects 12 entrance of dissolving tank, 13 entrance of the outlet of dissolving tank 12 connection solution force (forcing) pump, solution pressurization
13 outlet connection solution storage slot of pump, 14 entrance, the outlet of solution storage slot 14 connection 15 entrance of solution transfer pump, solution transfer pump
15 outlet connection hydrolysis 16 entrances of heat exchanger, 17 entrance of hydrolysis heat exchanger 16 outlet connection solution hydrolyzer, solution hydrolyzer 17
Outlet connection SCR denitration device；Solution hydrolyzer 17 is equipped with steam inlet connection turbine low pressure cylinder pumping, solution hydrolyzer 17
Raffinate outlet with hydrolysis heat exchanger 16 connect, hydrolyze heat exchanger 16 raffinate export divides two-way, connect all the way with dissolving tank 12,
Extra raffinate is discharged in another way.
The boiler tail equipment arrangement system of the present invention also slows down catalysis under the premise of meeting denitration efficiency
Agent inactivation and air preheater block.
As shown in Figure 1, a kind of method for slowing down SCR catalyst inactivation and air preheater and blocking of the present invention, including it is as follows
Step：
Boiler low-temperature superheater outlet flue gas passes sequentially through economizer 1 first and high-temperature air preheater 2 exchanges heat, high
The flue gas exit temperature of warm air preheater 2 is about 200 DEG C, and subsequent flue gas, which enters in electrostatic precipitator 3, removes coal ash particle
And most of coal ash dust, the flue gas after dust removal process enters SCR denitration device 4, in SCR denitration device 4 in flue gas
The ammonia and nitric acid gas that NO is injected into are restored, and the exiting flue gas of SCR denitration device 4 passes sequentially through Cryogenic air preheating again
Device 5 and steam air heater 6 carry out a Secondary Air of heating boiler, and it is about 80 DEG C that steam air heater 6, which exports smoke temperature, subsequently enters cold precipitator 7
In further remove fine dust particles object in flue gas, the flue gas after low temperature dedusting subsequently enters desulfurizing tower 8 and removes flue gas
In SO2, last flue gas is discharged into air via chimney 9.Wherein,
Urea conveyer 10 and nitric acid/ammonium nitrate conveyer 11 are according to 1:1 molar ratio is respectively urea and ammonium nitrate
It is transported in dissolving tank 12, agitated wiring solution-forming (or urea conveyer 10 and nitric acid/ammonium nitrate conveyer 11 are according to 1.5:1
Molar ratio urea and nitric acid are transported in dissolving tank 12 respectively, agitated wiring solution-forming), followed by solution force (forcing) pump
13 are transported to the mixed solution of urea and ammonium nitrate in solution storage slot 14, are forced into gauge pressure 2.6MPa or so, followed by
Mixed solution is transported in hydrolysis heat exchanger 16 by solution transfer pump 15, and is changed with the raffinate from solution hydrolyzer 17 out
Heat, the mixed solution that hydrolysis heat exchanger 16 exports are heated to about 180 DEG C, and decomposing ammonium nitrate is NH at this time3And HNO3, then mixed
It closes solution and is transported to solution hydrolyzer 17, the water of urea directly occurs for mixed solution and the steam extracted from turbine low pressure cylinder
Solution reaction, generates NH3, and the NH generated with decomposing ammonium nitrate before3And HNO3It sprays into SCR denitration device 4, then passes through together
NO in reaction reduction flue gas below：HNO3+2NO+3NH3→3N2+5H2O, denitration efficiency of the reaction at 200 DEG C are reachable
90%；
It is molten to be introduced into the hydrolysis heating mixing of heat exchanger 16 for about 200 DEG C of Residue temperature being discharged from 17 bottom of solution hydrolyzer
The Residue temperature of liquid, outlet is down to 90 DEG C or so, enters back into lytic agent of the dissolving tank 12 as urea and ammonium nitrate, and extra is residual
Liquid is sent to sewage plant processing.
What the present invention announced slows down the method that SCR catalyst inactivation and air preheater block, by adding in reducing agent
Enter ammonium nitrate, it is ensured that SCR denitration device meets institute's public address system of the present invention and react temperature to SCR in 200 DEG C of Effec-tive Functions
The requirement of degree and denitration efficiency.
In short, before and after by the way that air preheater is arranged in SCR device, deduster is placed in the cloth before SCR
Set the blocking of the inactivation and air preheater that can effectively slow down catalyst；At this point, the flue-gas temperature in SCR reactors is about
200 DEG C, then the efficiency that SCR reacts can be made 200 by the method for the addition ammonium nitrate (or nitric acid) into denitrification reducing agent
Reach requirement at DEG C.
Claims (9)
1. a kind of system for slowing down SCR catalyst inactivation and air preheater and blocking, it is characterised in that：Including being used for tail flue gas
Heat exchange and the flow of flue gas system purified and the reducing agent supply system that reducing agent is provided for SCR denitration reaction；
The flow of flue gas system includes connecting the economizer (1) of boiler low-temperature superheater outlet flue gas, the cigarette of economizer (1)
Gas outlet is connect with high-temperature air preheater (2), and the exhanst gas outlet of high-temperature air preheater (2) is connect with electrostatic precipitator (3),
Electrostatic precipitator (3) outlet is connect with SCR denitration device (4), and SCR denitration device (4) outlet connects with low-temperature air preheater (5)
It connects, the exhanst gas outlet of low-temperature air preheater (5) is connect with steam air heater (6), and steam air heater (6) outlet connects with cold precipitator (7)
It connects, cold precipitator (7) outlet is connect with desulfurizing tower (8), and desulfurizing tower (8) outlet is connect with chimney (9)；
The reducing agent supply system includes the dissolving tank of connection urea conveyer (10) and nitric acid/ammonium nitrate conveyer (11)
(12), dissolving tank (12) outlet is connect through solution force (forcing) pump (13) with solution storage slot (14), solution storage slot (14) outlet warp
Solution transfer pump (15) is connect with hydrolysis heat exchanger (16), and hydrolysis heat exchanger (16) is exported to be connected with the entrance of solution hydrolyzer (17)
It connects, solution hydrolyzer (17) outlet is connect with SCR denitration device (4).
2. the system as described in claim 1 for slowing down SCR catalyst inactivation and air preheater and blocking, it is characterised in that：Institute
Pressure fan (18) is also associated on the steam air heater (6) stated, steam air heater (6) air outlet slit is connect with low-temperature air preheater (5), low
The air outlet slit of warm air preheater (5) is connect with high-temperature air preheater (2), the air outlet slit of high-temperature air preheater (2)
It is connected to burner hearth.
3. the system as described in claim 1 for slowing down SCR catalyst inactivation and air preheater and blocking, it is characterised in that：Institute
The solution hydrolyzer (17) stated be equipped with steam inlet connection turbine low pressure cylinder pumping, solution hydrolyzer (17) raffinate outlet with
It hydrolyzes heat exchanger (16) to connect, the raffinate outlet of hydrolysis heat exchanger (16) divides two-way, connect with dissolving tank (12) all the way, another way
Extra raffinate is discharged.
4. a kind of method for slowing down SCR catalyst inactivation and air preheater and blocking of system as described in claim 1, feature
It is, includes the following steps：
Boiler low-temperature superheater outlet flue gas passes sequentially through economizer (1) first and high-temperature air preheater (2) exchanges heat, high
The flue gas exit temperature of warm air preheater (2) is about 200 DEG C, and subsequent flue gas enters electrostatic precipitator (3) and removes coal ash
Grain and most of coal ash dust, the flue gas after dust removal process enter SCR denitration device (4), the cigarette in SCR denitration device (4)
The ammonia and nitric acid gas that NO in gas is injected into are restored, and the exiting flue gas of SCR denitration device (4) passes sequentially through low temperature again
One Secondary Air of air preheater (5) and steam air heater (6) heating boiler, it is about 80 DEG C that steam air heater (6), which exports smoke temperature, is subsequently entered
Cold precipitator (7) removes the fine dust particles object in flue gas, and the flue gas after low temperature dedusting enters back into desulfurizing tower (8) removing
SO in flue gas2, last flue gas is discharged into air via chimney (9)；
Urea and nitric acid or ammonium nitrate are transported to dissolving tank by urea conveyer (10) and nitric acid/ammonium nitrate conveyer (11) respectively
(12) agitated wiring solution-forming in is then conveyed the mixed solution of urea, nitric acid or ammonium nitrate using solution force (forcing) pump (13)
It is 2.6MPa to pressure is forced into solution storage slot (14), hydrolysis heat exchanger (16) is then transported to by solution transfer pump (15)
It exchanging heat with the raffinate that solution hydrolyzer (17) comes out, the mixed solution that hydrolysis heat exchanger (16) exports is heated to about 180 DEG C, this
When nitric acid or decomposing ammonium nitrate be NH3And HNO3, subsequent mixed solution is transported to solution hydrolyzer (17), by steam turbine low-pressure
The cylinder bottom that the steam that cylinder extracts is passed through solution hydrolyzer (17) directly mixes the hydrolysis generation NH for carrying out urea with solution3,
The NH generated again with nitric acid before or decomposing ammonium nitrate3And HNO3It sprays into together and denitration reaction occurs in SCR denitration device (4).
5. the method as claimed in claim 4 for slowing down SCR catalyst inactivation and air preheater and blocking, it is characterised in that：Institute
The molar ratio of the urea and ammonium nitrate stated is 1:1.
6. the method as claimed in claim 4 for slowing down SCR catalyst inactivation and air preheater and blocking, it is characterised in that：Institute
The molar ratio of the urea and nitric acid stated is 1.5:1.
7. the method as claimed in claim 4 for slowing down SCR catalyst inactivation and air preheater and blocking, it is characterised in that：From
About 200 DEG C of the Residue temperature of solution hydrolyzer (17) bottom discharge is introduced into hydrolysis heat exchanger (16) and heats mixed solution, hydrolysis
The Residue temperature of heat exchanger (16) outlet is down to 90 DEG C or so and enters dissolving tank (12), and extra raffinate is sent to sewage plant processing.
8. the method as claimed in claim 4 for slowing down SCR catalyst inactivation and air preheater and blocking, it is characterised in that：Institute
The denitration reaction occurred in the SCR denitration equipment stated is：HNO3+2NO+3NH3→3N2+5H2O, the reaction are de- at 200 DEG C
Nitre efficiency is up to 90%.
9. the method as claimed in claim 4 for slowing down SCR catalyst inactivation and air preheater and blocking, it is characterised in that：Institute
The air stated is conveyed by pressure fan (18), passes sequentially through steam air heater (6), low-temperature air preheater (5), high-temperature air preheater
(2), the primary and secondary air after heat absorption heating as coal dust firing is sent into burner hearth.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611192800.3A CN106705091B (en) | 2016-12-21 | 2016-12-21 | A kind of system and method for slowing down SCR catalyst inactivation and air preheater and blocking |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611192800.3A CN106705091B (en) | 2016-12-21 | 2016-12-21 | A kind of system and method for slowing down SCR catalyst inactivation and air preheater and blocking |
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| CN106705091A CN106705091A (en) | 2017-05-24 |
| CN106705091B true CN106705091B (en) | 2018-08-28 |
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