CN106765246B - A kind of online method and device for removing refinery's FCC apparatus waste heat boiler fouling - Google Patents
A kind of online method and device for removing refinery's FCC apparatus waste heat boiler fouling Download PDFInfo
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- CN106765246B CN106765246B CN201510800795.9A CN201510800795A CN106765246B CN 106765246 B CN106765246 B CN 106765246B CN 201510800795 A CN201510800795 A CN 201510800795A CN 106765246 B CN106765246 B CN 106765246B
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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
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
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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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- 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
- F23J15/08—Arrangements of devices for treating smoke or fumes of heaters
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
- B01D2255/207—Transition metals
- B01D2255/20707—Titanium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
- B01D2255/207—Transition metals
- B01D2255/20723—Vanadium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
- B01D2255/207—Transition metals
- B01D2255/20769—Molybdenum
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
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- B01D2255/20776—Tungsten
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Abstract
The present invention relates to a kind of online methods for removing refinery's FCC apparatus waste heat boiler ammonium hydrogen sulfate fouling, according to flow of flue gas direction, it is equipped with combustion chamber successively in waste heat boiler, hyperthermia and superheating section, cryogenic overheating section, high temperature evaporation section, SCR denitration section, low-temperature evaporation section, high-temperature economizer and low-level (stack-gas) economizer, two-way high-temperature flue gas is drawn at waste heat boiler combustion chamber rear portion, wherein first via high-temperature flue gas is mixed with the flue gas after high temperature evaporation section, flue-gas temperature reaches 350~400 DEG C after making mixing, reduce the generation of ammonium hydrogen sulfate, denitration process is carried out subsequently into SCR denitration section；Another way high-temperature flue gas is mixed with the flue gas after low-temperature evaporation section, and flue-gas temperature reaches 400~470 DEG C after making mixing, then enters high-temperature economizer together, is made to condense in the ammonium hydrogen sulfate gasification on economizer boiler tube and is decomposed, achievees the purpose that remove fouling.The present invention can effectively prevent ammonium hydrogen sulfate to block FCC apparatus Economizer of Heat Recovery Boiler, reduce waste heat boiler raised pressure drop due to the blocking of economizer ammonium hydrogen sulfate, reach efficient deashing purpose, and do not influence the normal operation of boiler.
Description
Technical field
The present invention relates to refinery FCC apparatus exhaust-heat boiler flue gas denitration technology fields, and in particular to a kind of online removing refining
The method and device of factory's FCC apparatus П shape waste heat boiler ammonium hydrogen sulfate foulings.
Background technology
Nitrogen oxides, that is, NOx, it is one of primary pollution source of atmosphere pollution, primarily forms nitric acid type acid rain, is to form light
Chemical fumes mainly generates one of object.In oil plant, catalytic cracking（FCC）The regenerated flue gas of device discharge is main NOx
Emission source, annual emissions are in terms of ton.Since environmental protection standard is increasingly strict, FCC waste heat boilers are provided with denitration unit, denitration list
It is first mainly to use SCR denitration technique, it is to develop faster gas denitrifying technology in recent years.SCR（Selective
Catalytic Reduction）As SCR technology refers to existing in the effect of denitrating catalyst and oxygen
Under, NH3Reduction reaction occurs with NOx in flue gas, generates nitrogen and water, key reaction formula is：
4NO+4NH3+O2→4N2+6H2O
2NO2+4NH3 +O2→ N2+6H2O
The requirement of SCR denitration technique is control the escaping of ammonia can lead to unreacted NH if escape ammonia is excessively high3With flue gas
In SO3And H2O reaction generate ammonium hydrogen sulfate, ammonium hydrogen sulfate be cause Denitration in Boiler reactor downstream heat exchanging segment block it is main
Factor, reaction equation are as follows：
NH3+ SO3+ H2O→（NH4）HSO4
The fusing point of ammonium hydrogen sulfate is 147 DEG C, and boiling point is 350 DEG C, it is considered that ammonium hydrogen sulfate deposition temperature range be
150-270 DEG C, deposition region is usually on the fin heat exchange pipe in Benitration reactor downstream.Have in the ammonium hydrogen sulfate of this temperature range
There is stickiness, can largely adsorb the ash content in flue gas, there is strong corrosivity, heat exchange pipe fitting can be corroded.Result of study shows,
Ammonium hydrogen sulfate has part to decompose slowly to NH at 200 DEG C or more3And H2SO4, become gaseous state, big portion in >=350 DEG C of ammonium hydrogen sulfates
It decomposes but does not decompose thoroughly, at >=400 DEG C, ammonium hydrogen sulfate is just thoroughly decomposed into NH3And H2SO4。
SCR denitration technique is mainly used for the denitrating flue gas of refinery's waste heat boiler and the coal-burning boiler in power station.SCR denitration system
The SO of middle flue gas3And NH3It cannot eliminate, so the generation of ammonium hydrogen sulfate is inevitable.Since SCR denitration system comes into operation, when serious
The ammonium hydrogen sulfate of generation can cause the heat exchanging segment after Benitration reactor to block, and can cause boiler shutdown, removing used at present
Means, which are blowing outs, to be made to restore room temperature in stove, is then used the ammonium hydrogen sulfate fouling on high pressure water washing boiler tube fin, is influenced boiler
Normal operation.
Coal-burning boiler refers to fire coal combustion heat release amount in burner hearth, and heat medium water or other organic heat carriers are heated to one
Constant temperature degree（Or pressure）Thermal powerplant.Coal-burning boiler is typically provided with more than two air preheats in denitration unit downstream
Device, major function are to enter the air of boiler furnace using flue gas, and flue gas is general by the temperature of air preheater
It is 170~230 DEG C.Fire coal boiler fume flows to：Boiler economizer section → SCR → air preheater → electric precipitator → air inducing
Machine → wet method fume desulfurizing system → chimney.The negative pressure of air-introduced machine acting as in holding boiler, and give smoke power.It is combustion-supporting
Air flows to：Combustion air → air preheater → combustion chamber act as auxiliary burning of coal.
CN102042605A discloses a kind of hot ash removal method in coal-burning boiler rotary regenerative air preheater point side, this method profit
The pressure fan and air-introduced machine of an air preheater side are closed, by air preheater in boiler at low load with night generating set underload
Load pours into another air preheater, allows flue gas all to walk an air preheater, and reduce the air capacity of single air preheater, makes by empty pre-
The flue-gas temperature of device makes the ammonium hydrogen sulfate of the fouling on boiler tube decompose, achievees the purpose that removing to ammonium hydrogen sulfate dew point is much larger than.
The invention can periodically remove in, the dust stratification of low-temperature zone heat transfer element, make dust stratification be unlikely to develop to severity.But it should
Method needs that at least two groups air preheater is arranged, and needs side boiler carrying out cycling service, and operating process is cumbersome, no
It is convenient；And it is limited for the flue-gas temperature leeway for adjusting evaporation ammonium hydrogen sulfate, the too low evaporation ammonium hydrogen sulfate ability of temperature is not yet
It is enough.
CN104180378A discloses a kind of method that online elimination coal fired boiler of power plant air preheater ammonium hydrogen sulfate blocks up ash,
This process employs the peak load regulation underload periods, according to the reversibility pricinple of ammonium hydrogen sulfate deposition process, it is proposed that Yi Zhongyun
Row method of adjustment makes unilateral air preheater isolation air, is passed through a small amount of high-temperature flue gas, steps up air preheater global facility temperature,
Make to be attached to the liquid sulfuric acid hydrogen ammonium gasification on heat transfer element, is blocked to eliminate.The coal unit peak regulation in China is frequent at present,
Often there are long-time underrun period, such unit that can be frequently utilized that the underload peak regulation period at night, to empty pre-
Device carries out ammonium hydrogen sulfate in turn and blocks up ash cleaning, reduces air preheater resistance, avoids shutting down progress high pressure water washing, reduces economic damage
It loses.But the method needs to be provided at least two groups air preheater, and need side boiler carrying out cycling service, behaviour
It is cumbersome to make process, inconvenient and limited for the flue-gas temperature leeway for adjusting evaporation ammonium hydrogen sulfate, the too low evaporation sulfuric acid of temperature
Hydrogen ammonium ability is also inadequate.
CN104033921A discloses a kind of device and method for preventing ammonium hydrogen sulfate from blocking coal-burning boiler air preheater,
This method controls air preheater flue gas according to the sulfur content in coal-burning boiler as-fired coal, denitration facility exit ammonia slip concentration
The mass flow ratio of side entrance flue gas and air preheater air side intake air makes in air preheater fume side outlet temperature
210~320 DEG C are risen to, the flue gas communicating door on air preheater to the pipeline of deduster is opened simultaneously, makes deduster entrance temperature
≤ 160 DEG C of degree, achievees the purpose that removing.The invention can be effectively prevented the ammonium hydrogen sulfate brought by denitrating flue gas and block combustion
It the problem of coal burning boiler air preheater, on the other hand can be to avoid flue-gas temperature raising pair by being arranged and adjusting flue gas communicating door
The influence of deduster especially sack cleaner is conducive to the normal operation of coal-burning boiler, but for adjusting evaporation ammonium hydrogen sulfate
Flue-gas temperature leeway it is limited, the too low evaporation ammonium hydrogen sulfate ability of temperature is inadequate.
Above-mentioned patent contributes to coal-burning boiler, and refinery's FCC waste heat boilers are different from coal-burning boiler.Waste heat boiler is most
For П shape structures, burner hearth is adiabatic furnace structure, mostly uses finned tube in stove now as heat transfer element, regenerated flue gas and combustion-supporting
Wind enters from burner hearth bottom, arranges that water conservation section, back-end ductwork are sequentially arranged high/low temperature overheat on the horizontal flue of furnace outlet
The heating surfaces equipment such as device, convection current evaporator section, high/low temperature economizer, flue gas are discharged by back-end ductwork bottom.Refinery FCC waste heat pots
Stove, fuel is fuel oil or high pressure gas, and air-breathing is added, it is therefore an objective to the CO in FCC regenerator flue gas burnt up,
The combustion heat for recycling CO simultaneously, hot steam is pressed through in production.Conventional refinery catalytic cracking unit（FCC）Regenerated flue gas flow direction
For：FCC regenerators（0.3MPa）→ flue gas turbine expander → waste heat boiler（Inside set denitration unit）→ air preheater → desulfurization unit
→ chimney.Flue gas flow direction wherein in waste heat boiler is：Combustion chamber → water conservation section → high/low temperature superheat section → high/low temperature pair
Outside flow evaporator section → SCR → high/low temperature economizer section → stove.Gas and combustion air enter from furnace bottom burns up CO in combustion chamber.
Due to the difference of boiler structure, action function and associated component, the difference of coal-burning boiler and waste heat boiler is in particular in：
（1）Flue gas system pressure states are different：The pressure of fire coal boiler fume system is negative pressure, needs to set before chimney and draw
Wind turbine drawing smoke is into smoke stack emission.And refinery's FCC afterheat boiler systems are positive pressure, when refinery catalytic cracking catalyst regeneration by
Main compressor air feed, after burning flue gas pressures it is general >=0.3MPa, after smoke machine recovers energy, have into exhaust-heat boiler flue gas pressure
Positive pressure 10KPa is not provided with air-introduced machine, Wu Fayi so flue gas is discharged into smoke stack emission by exhaust-heat boiler flue gas by system pressure
By increasing wind turbine or adjustment air quantity, flue-gas temperature is improved to decompose ammonium hydrogen sulfate, is accordingly used in the control measures of negative pressure stove not
Suitable for positive pressure type waste heat boiler.
（2）Exhaust gas dust concentration is different：In refinery's FCC exhaust-heat boiler flue gas dust concentration≤1g/Nm3, general to only have
100~500mg/Nm3, main cause is that FCC regenerators are generally equipped with 1~3 grade of cyclone dust collectors dedusting, so regenerated flue gas powder
Dust content is low.Fire coal boiler fume dust concentration reaches 20~50g/Nm3, mainly generated after coal combustion.Due to exhaust gas dust
Concentration is different, causes the position that waste heat boiler and coal-burning boiler generate ammonium hydrogen sulfate different, waste heat boiler cannot draw by adjusting
Wind turbine or pressure fan adjust flue-gas temperature, and then adjust air preheater temperature, to reach deashing purpose.
（3）The ammonium hydrogen sulfate blocking of fire coal boiler fume system is happened at 170~230 DEG C of air preheater.And refinery
The ammonium hydrogen sulfate blocking of FCC exhaust-heat boiler flue gas systems is happened at 240~270 DEG C of economizer.Due to waste heat boiler denitration list
Without air preheater, typically just senior middle school's low-level (stack-gas) economizer after member, therefore flue-gas temperature is adjusted by air-introduced machine and pressure fan
Purge mode, be not particularly suited for waste heat boiler.
In summary, the minimizing technology suitable for negative-pressure type coal-burning boiler ammonium hydrogen sulfate is not appropriate for refinery's positive pressure type waste heat
Boiler needs to seek to remove technique online suitable for the ammonium hydrogen sulfate of FCC waste heat boilers.
Invention content
In view of the deficiencies of the prior art, the present invention provides a kind of online removing refinery's FCC apparatus waste heat boiler hydrogen sulfates
The method and device of ammonium fouling.The present invention can effectively prevent ammonium hydrogen sulfate to block FCC apparatus Economizer of Heat Recovery Boiler, more than reduction
Heat boiler raised pressure drop due to the blocking of economizer ammonium hydrogen sulfate, reaches efficient deashing purpose, and do not influence boiler just
Often operation.
The method that the present invention removes refinery's FCC apparatus waste heat boiler ammonium hydrogen sulfate fouling online, including following content：According to
Flow of flue gas direction, in П shape waste heat boilers successively be equipped with combustion chamber, hyperthermia and superheating section, cryogenic overheating section, high temperature evaporation section,
SCR denitration section, low-temperature evaporation section, high-temperature economizer and low-level (stack-gas) economizer draw two-way high temperature at waste heat boiler combustion chamber rear portion
Flue gas, wherein first via high-temperature flue gas are mixed with the flue gas after high temperature evaporation section, and flue-gas temperature reaches 350~400 after making mixing
DEG C, the generation of ammonium hydrogen sulfate is reduced, denitration process is carried out subsequently into SCR denitration section；Another way high-temperature flue gas and low-temperature evaporation
Flue gas mixing after section, flue-gas temperature reaches 400~470 DEG C after making mixing, then enters high-temperature economizer together, makes to condense in
Ammonium hydrogen sulfate gasification on economizer boiler tube is decomposed, and achievees the purpose that remove fouling.
In the present invention, the combustion temperature in hearth of the waste heat boiler combustion chamber is 800~900 DEG C, excess air coefficient 1
~1.4.It it is 800~900 DEG C in the high-temperature flue-gas that waste heat boiler combustion chamber rear portion is drawn, CO contents are 3%~6%（v/v）,
Dust concentration is 0.2~1g/Nm3, and contain Cu, Fe, Ni, the V etc. for leading to waste heat boiler ammonium hydrogen sulfate fouling.
In the present invention, flue gas plate washer can be set respectively on the two-way high temperature flue gas pipeline of extraction, preferably set electric guard board
Door adjusts two bypass flue gas flows according to the aperture of baffle door, and controls total extraction high-temperature flue gas amount respectively, improves and has sulphur
The economizer entrance flue gas temperature of sour hydrogen ammonium fouling evaporates hydrogen sulfate to 400 ~ 470 DEG C.Specific implementation can be according to waste heat boiler
The economizer pressure drop of denitration unit downstream adjusts accordingly, when discovery since ammonium hydrogen sulfate fouling makes Economizer of Heat Recovery Boiler section pressure
At 1.5~2 times of a height of former pressure drop of falling-rising, controlling the amount of flue gas emission of extraction, to account for the volume ratio of total exhaust gas volumn be 1%~80%, preferably
It is 10%~50%；Baffle door is closed after pressure drop restores normal.The case where present invention can change according to furnace pressure drop at any time into
Row intermittently operated does not interfere with the normal operation of waste heat boiler.
In the present invention, high-temperature flue gas flow is controlled according to the aperture of baffle door, makes the first via high-temperature flue gas and height of extraction
Flue-gas temperature reaches 350~400 DEG C after the flue gas mixing of SCR denitration section will be entered after warm evaporator section.Using aforesaid operations, one
Aspect can be such that the ammonium hydrogen sulfate after burning in flue gas largely decomposes, the NH released3By denitrating catalyst using being gone back
Original reaction, makes NOx become N2, reduce the ammonium hydrogen sulfate content in flue gas when reaching economizer section；On the other hand cigarette can be improved
Temperature degree avoids the deposition of ammonium hydrogen sulfate, reduces the addition of high-temperature flue gas before the economizer of another No. 1, ensures waste heat boiler just
Often operation.
In the present invention, SCR denitration section is filled with SCR denitration, can be denitration catalyst commonly used in the art
Agent, it is preferred to use denitrating catalyst be active component be coated in honeycomb support on honeycomb catalyst, aperture be 1~
10mm, active component are transition metal oxide.Active component be specially the oxide of V, the oxide of Ti, W oxide and
The oxide of Mo, it is as follows that active component with oxide is calculated as honeycomb substrate quality：V（0.1wt%~4wt%）,Ti（1wt%~
90wt%）,W（1wt%~15wt%）And Mo（0.1wt%~10wt%）.
In the present invention, under normal circumstances, economizer input gas temperature is at 240~270 DEG C when not being passed through high-temperature flue gas, root
High-temperature flue gas flow is controlled according to the aperture of baffle door, the another way high-temperature flue gas of extraction is made to be mixed with the flue gas after low-temperature evaporation section
Flue-gas temperature reaches 400~470 DEG C afterwards, then enters high-temperature economizer together, and processing time is set as 0.1~5h, makes condensation
Ammonium hydrogen sulfate gasification on economizer boiler tube is decomposed, and is taken away by boiler smoke.
A kind of device for above-mentioned online removing refinery's FCC apparatus ∏ type waste heat boiler ammonium hydrogen sulfate foulings, in ∏ types
Combustion chamber, hyperthermia and superheating section, cryogenic overheating section, high temperature evaporation section, SCR denitration section, low-temperature evaporation are equipped in waste heat boiler successively
Section, high-temperature economizer and low-level (stack-gas) economizer draw two-way high-temperature flue gas, first via high temperature at the shape waste heat boiler combustion chambers П rear portion
Flue gas is mixed with the flue gas after high temperature evaporation section, and flue-gas temperature reaches 350~400 DEG C after making mixing, subsequently into SCR denitration section
Carry out denitration process；Another 1 road high-temperature flue gas is mixed with the flue gas after low-temperature evaporation section, make after mixing flue-gas temperature reach 400~
470 DEG C, then enter high-temperature economizer together, makes to condense in the ammonium hydrogen sulfate gasification on economizer boiler tube and decompose, reach removing
The purpose of fouling.
In the present invention, electric guard board door is respectively arranged on two-way pipeline, cigarette after changing and mix according to furnace pressure drop
The temperature of gas, the aperture of control baffle door.
In the present invention, the high and low temperature evaporator section of CO waste heat boilers is provided with the heat-exchange finned tube of 4~10m.Ammonia and cigarette
Gas can make full use of these heat-exchange finned tubes, reach well-mixed effect, be conducive in next step in SCR denitration module
Catalytic-reduction denitrified reaction, special ammonia/flue gas mixer need not be separately provided.
Compared with prior art, the present invention has the following advantages：
（1）The present invention is by drawing two bypass high-temperature flue gas, under the collective effect of 2 road flue gases, the sulfuric acid in flue gas
Hydrogen ammonium is effectively controlled, and avoids it from depositing the influence to follow-up heat transmission equipment, and the present invention can be at any time according to boiler pressure
The case where drop variation, carries out intermittently operated, does not interfere with the normal operation of waste heat boiler.
（2）Positive pressure type waste heat boiler air-introduced machine cannot be arranged in waste heat boiler and pressure fan increases waste heat boiler position cigarette
Temperature degree, and by be arranged two bypass high-temperature flue gas after, and using plate washer door adjust flue gas flow, easily controllable flue gas flow
And mixture temperature, operation are fairly simple.
（3）Adjustment air-introduced machine and pressure fan flue gas flow, can influence efficiency of combustion and pot when general coal-burning boiler high load capacity
Stove producing steam amount, the present invention need not adjust air-introduced machine or pressure fan flow, and waste heat boiler need not also be carried out to periodical fortune
Row can both prevent ammonium hydrogen sulfate from blocking FCC Economizer of Heat Recovery Boiler, reduce waste heat boiler since economizer ammonium hydrogen sulfate blocks
And raised pressure drop, reach efficient deashing purpose.
Description of the drawings
Fig. 1 is a kind of process flow chart of the method for the present invention；
In figure：The regenerated flue gas of 1-FCC devices, the combustion chambers 2-, 3- hyperthermia and superheating sections, 4- cryogenic overheating sections, 5- high temperature steam
Hair section, the electronic plate washer doors of 6-1/6-2-, 7-SCR denitration sections, 8- low-temperature evaporation sections, 9- high-temperature economizers, 10- low-level (stack-gas) economizers,
Flue gas after 11- denitrations, 12- waste heat boilers.
Specific implementation mode
The method of the present invention is described in detail with reference to the accompanying drawings and examples, but therefore the present invention is not caused to limit
System.
The present invention removes the method and device such as attached drawing 1 of refinery's FCC apparatus ∏ type waste heat boiler ammonium hydrogen sulfate foulings online
It is shown, according to 1 flow direction of FCC apparatus regenerated flue gas, in waste heat boiler 12 successively be equipped with combustion chamber 2, hyperthermia and superheating section 3,
Cryogenic overheating section 4, high temperature evaporation section 5, SCR denitration section 7, low-temperature evaporation section 8, high-temperature economizer 9 and low-level (stack-gas) economizer 10, remaining
Two-way high-temperature flue gas is drawn at heat boiler combustion chamber rear portion, wherein will enter denitration after first via high-temperature flue gas and high temperature evaporation section
The flue gas of catalyst bed mixes, and flue-gas temperature reaches 350~400 DEG C after making mixing, and denitration is carried out subsequently into SCR denitration section
Processing；Another way high-temperature flue gas is mixed with the flue gas after low-temperature evaporation section so that and flue-gas temperature reaches 400~470 DEG C after mixing,
Then enter high-temperature economizer together, make to condense in the ammonium hydrogen sulfate gasification on economizer boiler tube and decompose, reach and remove fouling
Processing unit is discharged in purpose, the flue gas 11 after denitration.
The present invention is respectively arranged with electric guard board door 6-1 and 6-2 on two-way pipeline, is changed according to furnace pressure drop and is mixed
The temperature of flue gas afterwards, the aperture of control baffle door.
The present invention is provided with the heat-exchange finned tube of 6m in the high and low temperature evaporator section of CO waste heat boilers.
SCR denitration section of the present invention is filled with SCR denitration, and denitrating catalyst is that active component is coated in cellular load
Denitrating catalyst on body, aperture 5mm.Active component is transition metal oxide, specially the oxidation of the oxide of V, Ti
It is as follows to be calculated as honeycomb substrate quality with oxide for the oxide of object, the oxide of W and Mo：V：2wt%,Ti：90wt%,W：7wt%
And Mo：0.5wt%, the catalyst have good catalytic activity to SCR reactions.
Embodiment 1
Certain refinery CO waste heat boiler parameters：160,000 Nm of regenerated flue gas flow3/ h, 510 DEG C of temperature, CO contents 6%（v/v）.Its
Design thermal efficiency 77%, regenerated flue gas temperature after hearth combustion is 813 DEG C, and excess air coefficient 1.2, CO contents are 3%（v/
v）, dust concentration 0.7g/Nm3, and contain Cu, Fe, Ni, the V etc. for leading to waste heat boiler ammonium hydrogen sulfate fouling.
Denitration unit denitration, 308 DEG C of denitration reaction temperature, after noting ammonia, by NOx by 800mg/Nm is added in the waste heat boiler3
It is down to 200mg/Nm3, after running 5 months, because it is found that ammonia excessively adds, the advanced economizer pressure drop of boiler rises from 600Pa
To 1800Pa, exhaust gas temperature rises to 195 DEG C by 175 DEG C, and analysis reason is that economizer generates ammonium hydrogen sulfate, and boiler is caused to save coal
Device section blocks fouling, and heat exchange efficiency is caused to decline, and needs progress economizer deashing that could restore boiler efficiency.It is blown using soot blower
Ash is ineffective, therefore the method for the present invention is used to carry out deashing.
Regenerated flue gas is warming up to 813 DEG C behind combustion chamber, draws two-way high-temperature flue gas at combustion chamber rear portion, controls extraction
The volume ratio that amount of flue gas emission accounts for total exhaust gas volumn is 10%.Wherein first via high-temperature flue gas leads to the outlet of high temperature evaporation section, after making mixing
Flue-gas temperature reaches 375 DEG C, and denitration process is carried out subsequently into SCR denitration section；After another way high-temperature flue gas and low-temperature evaporation section
Flue gas mixing, flue-gas temperature reaches 400 DEG C after making mixing, then enters high-temperature economizer together, after continuous service 4h, saves coal
Device pressure drop is down to 700Pa by 1800Pa, and pressure drop when basic recovery goes into operation closes baffle door, restores boiler normal operation at this time, from
And make to condense in the gasification of the ammonium hydrogen sulfate on economizer boiler tube and decompose, achieve the purpose that remove fouling.The pressure of boiler is monitored simultaneously
Drop, once find due to ammonium hydrogen sulfate fouling make Economizer of Heat Recovery Boiler section pressure drop increase be 900Pa when, open baffle door, weight
Multiple aforesaid operations.The case where present invention can change according to furnace pressure drop at any time carries out intermittently operated, does not interfere with waste heat boiler
Operation steady in a long-term.
Embodiment 2
Certain refinery CO waste heat boiler parameters：140,000 Nm of regenerated flue gas flow3/ h, 546 DEG C of temperature, CO contents 6.3%（v/v）.
Its design thermal efficiency 75%, regenerated flue gas temperature after hearth combustion is 800 DEG C, excess air coefficient 1.3, and CO contents are
3.2%（v/v）, dust concentration 0.6g/Nm3, and contain Cu, Fe, Ni, the V etc. for leading to waste heat boiler ammonium hydrogen sulfate fouling.
Denitration unit denitration, 313 DEG C of denitration reaction temperature, after noting ammonia, by NOx by 600mg/Nm is added in the waste heat boiler3
It is down to 150mg/Nm3, after running 5 months, because it is found that ammonia excessively adds, the advanced economizer pressure drop of boiler rises from 800Pa
To 1400Pa, exhaust gas temperature rises to 199 DEG C by 169 DEG C, and analysis reason is that economizer generates ammonium hydrogen sulfate, and boiler is caused to save coal
Device section blocks fouling, and heat exchange efficiency is caused to decline, and needs progress economizer deashing that could restore boiler efficiency.It is blown using soot blower
Ash is ineffective, therefore the method for the present invention is used to carry out deashing.
Regenerated flue gas is warming up to 800 DEG C behind combustion chamber, draws two-way high-temperature flue gas at combustion chamber rear portion, controls extraction
The volume ratio that amount of flue gas emission accounts for total exhaust gas volumn is 28%.Wherein first via high-temperature flue gas leads to the outlet of high temperature evaporation section, after making mixing
Flue-gas temperature reaches 358 DEG C, and denitration process is carried out subsequently into SCR denitration section；After another way high-temperature flue gas and low-temperature evaporation section
Flue gas mixing, flue-gas temperature reaches 410 DEG C after making mixing, then enters high-temperature economizer together, after continuous service 5h, saves coal
Device pressure drop is down to 800Pa by 1400Pa, and pressure drop when basic recovery goes into operation closes baffle door, restores boiler normal operation at this time, from
And make to condense in the gasification of the ammonium hydrogen sulfate on economizer boiler tube and decompose, achieve the purpose that remove fouling.The pressure of boiler is monitored simultaneously
Drop, once find due to ammonium hydrogen sulfate fouling make Economizer of Heat Recovery Boiler section pressure drop increase be 1000Pa when, open baffle door, weight
Multiple aforesaid operations.The case where present invention can change according to furnace pressure drop at any time carries out intermittently operated, does not interfere with waste heat boiler
Normal operation.
Embodiment 3
Certain refinery CO waste heat boiler parameters：100,000 Nm of regenerated flue gas flow3/ h, 532 DEG C of temperature, CO contents 6.2%（v/v）.
Its design thermal efficiency 75%, regenerated flue gas temperature after hearth combustion is 808 DEG C, excess air coefficient 1.4, and CO contents are
3.4%（v/v）, dust concentration 0.8g/Nm3, and contain Cu, Fe, Ni, the V etc. for leading to waste heat boiler ammonium hydrogen sulfate fouling.
Denitration unit denitration, 309 DEG C of denitration reaction temperature, after noting ammonia, by NOx by 700mg/Nm is added in the waste heat boiler3
It is down to 100mg/Nm3, after running 5 months, because it is found that ammonia excessively adds, the advanced economizer pressure drop of boiler rises from 650Pa
To 1700Pa, exhaust gas temperature rises to 210 DEG C by 166 DEG C, and analysis reason is that economizer generates ammonium hydrogen sulfate, and boiler is caused to save coal
Device section blocks fouling, and heat exchange efficiency is caused to decline, and needs progress economizer deashing that could restore boiler efficiency.It is blown using soot blower
Ash is ineffective, therefore the method for the present invention is used to carry out deashing.
Regenerated flue gas is warming up to 808 DEG C behind combustion chamber, draws two-way high-temperature flue gas at combustion chamber rear portion, controls extraction
The volume ratio that amount of flue gas emission accounts for total exhaust gas volumn is 37%.Wherein first via high-temperature flue gas leads to the outlet of high temperature evaporation section, after making mixing
Flue-gas temperature reaches 368 DEG C, and denitration process is carried out subsequently into SCR denitration section；After another way high-temperature flue gas and low-temperature evaporation section
Flue gas mixing, flue-gas temperature reaches 418 DEG C after making mixing, then enters high-temperature economizer together, after continuous service 5h, saves coal
Device pressure drop is down to 700Pa by 1700Pa, and pressure drop when basic recovery goes into operation closes baffle door, restores boiler normal operation at this time, from
And make to condense in the gasification of the ammonium hydrogen sulfate on economizer boiler tube and decompose, achieve the purpose that remove fouling.The pressure of boiler is monitored simultaneously
Drop, once find due to ammonium hydrogen sulfate fouling make Economizer of Heat Recovery Boiler section pressure drop increase be 900Pa when, open baffle door, weight
Multiple aforesaid operations.The case where present invention can change according to furnace pressure drop at any time carries out intermittently operated, does not interfere with waste heat boiler
Normal operation.
Comparative example 1
Treatment process and operating condition with embodiment 3, the difference is that：It only draws high-temperature flue gas all the way and leads to high temperature steaming
Send out section outlet, flue-gas temperature reaches 368 DEG C after making mixing, subsequently into SCR denitration section carry out denitration process, economizer pressure drop by
1700Pa is down to 1500Pa, and treatment effect is bad.
Comparative example 2
Treatment process and operating condition with embodiment 3, the difference is that：Only draw high-temperature flue gas and low-temperature evaporation all the way
Flue gas mixing after section, flue-gas temperature reaches 418 DEG C after making mixing, then enters high-temperature economizer together, after continuous service 5h,
Economizer pressure drop is down to 1300Pa by 1700Pa, and treatment effect is bad.
Comparative example 3
Treatment process and operating condition with embodiment 3, the difference is that：Waste heat boiler is changed to coal-burning boiler, stove
Interior negative pressure≤2KPa, pressure are less than waste heat boiler, 160,000 Nm of flue gas flow3/ h, excess air coefficient 1.2 design thermal effect
Rate 72%.After being handled using method of the present invention, treatment effect is bad, and influences the normal operation of boiler.On the one hand by
In coal-burning boiler be negative pressure stove, but pressure drop in furnace it is general≤2000Pa, be much smaller than waste heat boiler, after the present invention program, by
It is small in differential pressure, therefore need to increase baffle door aperture, bypass flue gas flow could be increased, be affected to boiler.On the other hand, by
Big in fire coal boiler fume Dust Capacity, up to 40~50g/Nm3 is increased gas bypass, can be made after the present invention program
Flue is denuded, and leads to smoke spillage, in addition Dust Capacity is big, gas bypass may be caused to block.
Claims (11)
1. a kind of online method for removing refinery's FCC apparatus waste heat boiler ammonium hydrogen sulfate fouling, it is characterised in that in following
Hold：According to flow of flue gas direction, it is equipped with combustion chamber, hyperthermia and superheating section, cryogenic overheating section, high temperature successively in П shape waste heat boilers
Evaporator section, SCR denitration section, low-temperature evaporation section, high-temperature economizer and low-level (stack-gas) economizer draw two at waste heat boiler combustion chamber rear portion
Road high-temperature flue gas, wherein first via high-temperature flue gas are mixed with the flue gas after high temperature evaporation section, and flue-gas temperature reaches 350 after making mixing
~400 DEG C, the generation of ammonium hydrogen sulfate is reduced, denitration process is carried out subsequently into SCR denitration section；Another way high-temperature flue gas and low temperature
Flue gas mixing after evaporator section, flue-gas temperature reaches 400~470 DEG C after making mixing, then enters high-temperature economizer together, makes to coagulate
The ammonium hydrogen sulfate gasification tied on economizer boiler tube is decomposed, and achievees the purpose that remove fouling.
2. according to the method described in claim 1, it is characterized in that：The combustion temperature in hearth of the waste heat boiler combustion chamber is
800~900 DEG C, excess air coefficient is 1~1.4.
3. according to the method described in claim 1, it is characterized in that：In the high-temperature flue gas temperature that waste heat boiler combustion chamber rear portion is drawn
Degree is 800~900 DEG C, and CO contents are 3%~6%（v/v）, dust concentration is 0.2~1g/Nm3, and containing leading to waste heat boiler
Cu, Fe, Ni and V of ammonium hydrogen sulfate fouling.
4. according to the method described in claim 1, it is characterized in that：Flue gas is set respectively on the two-way high temperature flue gas pipeline of extraction
Plate washer adjusts separately two-way flue gas flow according to the aperture of baffle door, and controls total extraction exhaust gas volumn.
5. according to the method described in claim 4, it is characterized in that：According to the downstream economizer pressure drop of waste heat boiler denitration unit into
The corresponding adjustment of row, when discovery since ammonium hydrogen sulfate fouling makes Economizer of Heat Recovery Boiler section pressure drop raising for 1.5~2 times of former pressure drop
When, control extraction amount of flue gas emission account for total exhaust gas volumn volume ratio be 1%~80%；Baffle door is closed after pressure drop restores normal.
6. according to the method described in claim 4, it is characterized in that：High-temperature flue gas flow is controlled according to the aperture of baffle door, is made
Flue-gas temperature reaches after the first via high-temperature flue gas of extraction is mixed with the flue gas that will enter SCR denitration section after high temperature evaporation section
350~400 DEG C.
7. according to the method described in claim 4, it is characterized in that：Under normal circumstances, when not being passed through high-temperature flue gas economizer into
Mouth flue-gas temperature controls high-temperature flue gas flow at 240~270 DEG C, according to the aperture of baffle door, makes the another way high temperature cigarette of extraction
Flue-gas temperature reaches 400~470 DEG C after gas is mixed with the flue gas after low-temperature evaporation section, then enters high-temperature economizer, place together
The reason time is set as 0.1~5h, makes to condense in the ammonium hydrogen sulfate gasification on economizer boiler tube and decomposes, is taken away by boiler smoke.
8. according to the method described in claim 1, it is characterized in that：SCR denitration section is filled with SCR denitration, catalyst
It is coated in the honeycomb catalyst on honeycomb support for active component, aperture is 1~10mm, and active component is oxide, the Ti of V
Oxide, the oxide of W and the oxide of Mo, it is as follows that honeycomb substrate quality is calculated as with oxide：V：0.1wt%~4wt%,
Ti：1wt%~90wt%, W：1wt%~15wt%, Mo：0.1wt%~10wt%.
9. a kind of online device for removing refinery's FCC apparatus waste heat boiler ammonium hydrogen sulfate fouling, it is characterised in that：In ∏ type waste heats
Combustion chamber, hyperthermia and superheating section, cryogenic overheating section, high temperature evaporation section, SCR denitration section, low-temperature evaporation section, height are equipped in boiler successively
Warm economizer and low-level (stack-gas) economizer draw two-way high-temperature flue gas, first via high-temperature flue gas at the shape waste heat boiler combustion chambers П rear portion
It is mixed with the flue gas after high temperature evaporation section, flue-gas temperature reaches 350~400 DEG C after making mixing, reduces the generation of ammonium hydrogen sulfate, so
Enter SCR denitration section afterwards and carries out denitration process；Another 1 road high-temperature flue gas is mixed with the flue gas after low-temperature evaporation section, makes cigarette after mixing
Temperature degree reaches 400~470 DEG C, then enters high-temperature economizer together, makes to condense in the ammonium hydrogen sulfate gas on economizer boiler tube
Change and decompose, achievees the purpose that remove fouling.
10. device according to claim 9, it is characterised in that：Electric guard board door, root are respectively arranged on two-way pipeline
The temperature of flue gas, the aperture of control baffle door after changing and mix according to furnace pressure drop.
11. device according to claim 9, it is characterised in that：The high and low temperature evaporator section of CO waste heat boilers is provided with 4
The heat-exchange finned tube of~10m.
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| CN109681894A (en) * | 2018-12-04 | 2019-04-26 | 中材节能股份有限公司 | Clear up the process that industrial furnace Economizer of Heat Recovery Boiler ammonium hydrogen sulfate blocks up ash |
| CN110756049A (en) * | 2019-12-02 | 2020-02-07 | 南京凯盛国际工程有限公司 | Self-analysis SCR denitration system |
| CN111036192B (en) * | 2019-12-23 | 2021-08-06 | 中国科学院过程工程研究所 | Coating type wear-resistant vanadium denitration catalyst and preparation method and application thereof |
| CN112240556B (en) * | 2020-10-20 | 2022-11-01 | 江苏天楹等离子体科技有限公司 | Flue gas waste heat utilization device of garbage incinerator |
| CN114100349A (en) * | 2021-11-29 | 2022-03-01 | 大唐黄岛发电有限责任公司 | Pipeline device and method capable of performing pyrolysis of air preheater at any time |
| CN114278399A (en) * | 2021-12-29 | 2022-04-05 | 上海纳科助剂有限公司 | Method for preventing flue gas turbine from serious scaling in catalytic cracking process |
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| US4562795A (en) * | 1983-07-20 | 1986-01-07 | Firma Ferdinand Lentjes Dampfkessel- Und Maschinenbau | Process and equipment for reducing the emission of pollutants in flue gases from furnace installations |
| CN103104927A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Smoke denitration method of carbon monoxide (CO) heat recovery boiler of fluid catalytic cracking (FCC) device |
| CN103768932A (en) * | 2012-10-23 | 2014-05-07 | 中国石油化工股份有限公司 | Flue gas denitration process for CO exhaust-heat boiler of FCC apparatus |
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| US4562795A (en) * | 1983-07-20 | 1986-01-07 | Firma Ferdinand Lentjes Dampfkessel- Und Maschinenbau | Process and equipment for reducing the emission of pollutants in flue gases from furnace installations |
| CN103104927A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Smoke denitration method of carbon monoxide (CO) heat recovery boiler of fluid catalytic cracking (FCC) device |
| CN103768932A (en) * | 2012-10-23 | 2014-05-07 | 中国石油化工股份有限公司 | Flue gas denitration process for CO exhaust-heat boiler of FCC apparatus |
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