CN102309910A - Fluid catalytic cracking (FCC) flue gas treatment method - Google Patents

Fluid catalytic cracking (FCC) flue gas treatment method Download PDF

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Publication number
CN102309910A
CN102309910A CN2010102224121A CN201010222412A CN102309910A CN 102309910 A CN102309910 A CN 102309910A CN 2010102224121 A CN2010102224121 A CN 2010102224121A CN 201010222412 A CN201010222412 A CN 201010222412A CN 102309910 A CN102309910 A CN 102309910A
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flue gas
fcc
revolving bed
desulfurization
acid
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李勇
刘忠生
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China Petroleum and Chemical Corp
Sinopec Fushun Research Institute of Petroleum and Petrochemicals
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China Petroleum and Chemical Corp
Sinopec Fushun Research Institute of Petroleum and Petrochemicals
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    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Abstract

The invention discloses a fluid catalytic cracking (FCC) flue gas treatment method, which comprises the following steps of: mixing FCC flue gas and ammonia, performing selective reduction denitration reaction of NOx in the presence of a catalyst, performing revolving bed absorption desulfuration on the flue gas subjected to the selective reduction denitration reaction by using discharged water obtained after H2S is removed from acidic water as absorption liquid, further performing alkali liquid absorption desulfuration on the flue gas subjected to the revolving bed absorption desulfuration, discharging the flue gas, mixing the liquid phase discharged after the revolving bed absorption desulfuration and the acidic water to regulate the pH value of the acidic water to between 4 and 6, blowing out H2S by using air, burning the blown H2S in an incinerator, and treating the sewage in a sewage treatment plant after the H2S is blown out. By the method, the denitration and desulfuration processes of the FCC flue gas are finished; and the H2S in the acidic water is removed by using the obtained diluted acid, so that the acid consumption in the acidic water treatment is saved, and the acidic water treatment cost and the FCC flue gas treatment cost are reduced.

Description

A kind of FCC flue gas managing technique method
Technical field
The present invention relates to the improvement process of oil plant FCC flue gas, particularly relate to refinery FCC denitrating flue gas desulphurization technological process.
Background technology
NOx and SOx are one of primary pollution source of atmosphere pollution.NOx in the atmosphere and SOx are mainly from the discharging of tail gas such as the discharging gas of the industrial process relevant with combustion process and motor vehicles, steamer.
Nitrogen oxide is generically and collectively referred to as NOx, and what harm was maximum mainly is: NO, NO 2The main harm of NOx is following: (1) is to the effect of toxic elements in human body evil; (2) to the toxic effect of plant; (3) can form acid rain, acid mist; (4) form photochemical fog with hydrocarbon; (5) damage the ozone layer.
In atmosphere, SO 2Can oxidation form sulfuric acid mist or sulfate aerosol, be the important predecessor of environment acidifying.Sulfur dioxide concentration can make the breathing problem incidence of disease increase at >=0.5ppm in the atmosphere.
At oil plant, in FCC (fluid catalytic cracking) technology, catalyst granules is circulation repeatedly between catalytic cracking zone and catalyst regeneration zone.In catalyst regeneration process, the coke from cracking reaction on the catalyst granules is at high temperature removed through air oxidation, and the removal of deposits of coke recovers activity of such catalysts, and in cracking reaction, can be utilized again, and the tail gas that effluxes is the FCC flue gas.
The flue gas that NOx in the FCC flue gas and SOx almost all produce from the regenerative combustion on the catalyst.
NO and NO in the FCC flue gas 2All have, NO accounts for 90%, NO 2Account for 10%.NOx amount in the FCC flue gas generally accounts for 50% of refinery NOx discharge capacity, is the focus of location NOx discharging.
For the NOx discharging of control oil plant, all formulated corresponding discharge standard both at home and abroad.EPA and 13 tame oil refining enterprises have been signed pollutant control agreement (Consent Decree), and European Union requires all oil plants to carry out " comprehensive pollution and control guide ", and Japan has formulated the discharge standard of the NOx of FCCU.China " atmosphere comprehensive pollution thing discharge standard-GB16297-1996 " regulation: the highest permission concentration of emission of old pollution sources: NOx is 420mg/m 3, SO 2Be 700mg/m 3, new pollution sources are 240mg/m 3, SO 2Be 500mg/m 3, also formulate " petroleum refining industry pollutant emission standard " at present from the industry angle.
In recent years, along with the increase of imported crude oil amount, oil plant NOx pollution problem is serious day by day, along with the increasingly stringent of environmental regulation, the NOx discharge index is required to improve thereupon.Therefore, instant stage has been arrived in the NOx pollution control.
Improvement to flue gas is basically all adopted now: denitration → sulfur removal technology.In gas denitrifying technology, selective reduction (SCR) technology is compared with other technologies, has the denitration efficiency height, and advantages such as technology maturation are the at present domestic and international maximum technology of denitrating flue gas practical applications.It is low that other technologies are removed efficient like: SNCR (SNCR) method, and the escapement ratio of ammonia is high.The liquid absorption method denitration efficiency is low; The absorption method denitration efficiency is high, but adsorbance is little, and regeneration is frequent, uses wideless; High energy electron active oxidation method is desulphurization denitration simultaneously, but energy consumption is high, and the life-span is short.
The SCR method is meant 200 ℃~400 ℃ of reaction temperatures, uses NH 3Make reducing agent with NO xCatalytic reduction is N 2, the oxygen in the waste gas is seldom participated in reaction, and thermal discharge is little.With NH 3Doing the reaction of reducing agent can represent as follows:
4NH 3+6NO→5N 2+6H 2O+1806.6kJ
8NH 3+6NO 2→7N 2+12H 2O+2730.6kJ
CN1895744A has introduced a kind of high dirt composite SCR smoke denitrating technique and denitration catalyst reaction unit, and this cover SCR flow process is primarily aimed at the NOx in the power-plant flue gas, the NO of inapplicable FCC flue gas xAdminister.Its shortcoming shows: only consider how to remove NOx and the SO in the flue gas 2, do not consider how to carry out resource recycling and reduce alkaline consumption.Sulfur removal technology adopts wet desulphurization basically, and its main equipment is the reverse contact tower of flue gas-alkali lye, the alkali that wherein desulfurization consumed, with after promptly abandon, belong to the resource disposal type, the consumption of annual alkali is very big, every year is millions of mostly at least.
The a large amount of reverse contact towers of flue gas-alkali lye that use of flue gas desulfurization comprise packed column and plate column, and gas-liquid two-phase is to rely on the effect of gravitational field to realize contact mass transfer; But since gravitational field a little less than; Liquid film flows slowly, and effectively contact area is little in the unit volume, so mass-transfer efficiency is very low; Equipment volume is huge, and space availability ratio is low.
Early 1980s grow up high-gravity rotating bed be a kind of high efficient gas and liquid absorption equipment; Both improved absorption efficiency, and dwindled unit scale again, its cardinal principle is: in the rotary drill reactor; Gas is through being full of the whole rotor of liquid; Simultaneously whole rotor rotates together, and gas and liquid is under the centrifugal action of gravity, counter current contacting in rotor; Make that mass transfer, heat transfer or course of reaction between the gas-liquid two-phase are strengthened, reached the purpose that increases efficient, reduction equipment and cut down the consumption of energy.Should technology successfully be applied in the separation and operation of industrial process such as chemical industry, pharmacy both at home and abroad at present.The existing technology appearance that is used for revolving bed flue gas desulfurization.
The Yu Yun of Zhejiang Polytechnical University is good wait on " science and technology circular " 24 the 1st phases of volume in 2008, introduced a kind deflection type overgravity rotary bed; Utility model patent CN68867Y also discloses a kind of multilayer deflection type overgravity rotary bed, and both all can be used for gas-liquid contact occasion.
Summary of the invention
The invention provides a kind of refinery FCC flue gas managing technique, the denitration sulfur removal technology of FCC flue gas and acid water are removed H 2S technology organically combines, and reduces comprehensive regulation operating cost.
FCC flue gas managing technique of the present invention comprises following content: the FCC flue gas at first mixes with ammonia, in the presence of catalyst, carries out the selective reduction denitration reaction of NOx then, and the flue gas of process selective reduction denitration reaction adopts acid water to take off H 2Discharge water behind the S is that absorption liquid is rotated bed absorption desulfurization; The flue gas that revolving bed absorbs after the desulfurization further discharges after alkali lye absorbs desulfurization; Revolving bed absorbs the liquid phase of desulfurization discharge to be mixed with acid water, acid water pH value is adjusted to 4~6, and blows out H with air 2S, the H that blows out 2S goes incinerator to burn, and blows out H 2Sewage gets into the sewage-farm processing behind the S.
In the inventive method, the amount of the ammonia that mixes with the FCC flue gas is pressed 90%~110% of the required theoretical amount of NOx reduction reaction in the FCC flue gas and is confirmed.
In the inventive method, the flue gas after the denitration gets into the revolving bed absorption tower after heat exchanger heat exchange cooling, and absorption liquid adopts acid water to take off H 2Discharge water behind the S; The pH value of this discharge water is>=7, and SOx is absorbed the liquid efficient absorption in the flue gas in the revolving bed absorption tower, and revolving bed absorption tower outlet flue gas removes SOx remaining in the flue gas through the reverse contact tower of flue gas-alkali lye again; Flue gas after desulfurization discharges through chimney after demist.
The liquid phase that discharge on the revolving bed absorption tower is the diluted acid that absorbs SOx, and this diluted acid gets into H 2S removes reactor and transfers acid water pH to 4~6, the H of generation 2S is blown out by air, goes incinerator to burn, and the flue gas that contains SOx that obtains goes to the revolving bed absorption tower to reclaim SOx after the heat exchange cooling, goes the chimney discharging after the desulfurization, removes H 2Acid water behind the S (pH4~6) oil removing slagging-off is also transferred pH>=7.0 back decontaminated water treatment plants.
The present invention had both accomplished the technical process of the denitration desulfurization of FCC flue gas, and the diluted acid that obtains removes to remove H 2S, the H that removes 2The SOx that S burns the back generation removes to make diluted acid again, forms a SO 2The material consumption during acid water is administered has been saved in the circulation of recycling, and has reduced the processing cost of acid water.
Introduce technical process of the present invention below in detail: from the flue gas and the NH of FCC boiler 3, together get into flue gas-ammonia blender, fully mix NH with ammonia at this flue gas 3Amount size=NH 3NH that catalytic reduction reaction consumes takes place with NOx 3Amount, can slightly adjust according to process condition.
Ammonia after mixing-flue gas gaseous mixture gets into catalytic reduction reactor under 300 ℃~400 ℃, carries out catalytic reduction reaction and removes NOx, accomplishes the denitrating flue gas process.Described catalyst adopts alveolate texture, adopts TiO 2Be key component, add metals such as V, W, Fe, Mn, Ce, and adding appropriate amount of addition agent compacting roasting forms as the activity of such catalysts component.Reaction has good catalytic activity to this catalyst to SCR.Selective denitrification can adopt existing catalyst, and is of CN200910204252.5.
Under 300 ℃~400 ℃, NH 3Not with the SOx generation ammonium salt that reacts, the high-temperature flue gas of catalytic reduction reactor outlet reclaims fume afterheat through heat exchanger.Recovery waste heat can be used to produce materials such as steam or heating slurry oil.
Get into NH in the preceding flue gas of heat exchanger 3Be lower than 5mg/m 3, flue gas is through behind the heat exchanger, and flue-gas temperature is reduced to 100 ℃ even lower, is generally 60~150 ℃.
The advantage of flue gas cool-down is: improved the effect of the Gas-Liquid Absorption on revolving bed absorption tower after flue gas gets into, avoided high-temperature flue gas a large amount of water smokes that heat release produces when the gas-liquid contact mass transfer, influenced the phenomenon of Gas-Liquid Absorption effect, alleviated the load of demister.
Low-temperature flue gas after the heat exchange gets into the revolving bed absorption tower, and the acid water after the usefulness neutralization is as SO 2Absorption liquid, produce diluted acid, the diluted acid of production gets into sour tank stores.Dilute acid concentration scope 0.1%~10% (mass concentration).
Adopt the advantage of rotary drill reactor to be: because the revolving bed absorption tower is the high efficient gas and liquid absorption equipment, can dwindle unit scale, and improve absorption efficiency, on the basis that the absorption liquid measure does not increase, improve assimilation effect.
Remove most of SO 2Flue gas get into the reverse contact tower of flue gas-alkali lye and remove remaining SOx, accomplish the desulfurization control indexes, flue gets into the chimney discharging after getting into the demister demist.
From the diluted acid of storage tank and acid water from the acid water storage tank, in blender, mix, transfer pH to 4~6, the mixed liquor that mixes up pH through the heat exchanger cooling after, get into H 2S removes reactor and further reacts, and uses an amount of air aeration, makes H 2S overflows with air, through H 2After S gas divides the flow container separatory, go incinerator to burn.
Adopt the advantage of air aeration to be: control H 2S concentration range 0.1%~3% (volumetric concentration) can be avoided H 2The explosion limit of S.Incinerator burns to produce and contains SO 2Flue gas after the heat exchange cooling, turns back to the revolving bed absorption tower and removes to remove SO 2, after demist again, discharge by chimney.Absorption liquid absorbs SO 2After become the diluted acid of (mass concentration 0.1%~10%).
Take off H 2Acid water behind the S gets into settling tank and carries out the sedimentation layering.Oil slick sediment in the acid water is discharged from settling tank, and after acid water added adjusting PH with base >=7.0, part was returned the revolving bed absorption tower as absorption liquid system diluted acid, and remainder enters the sewage-farm and handles.
The present invention had both accomplished the technical process of the denitration desulfurization of FCC flue gas, and the diluted acid that obtains removes the H in the acid water again 2S has saved the alkaline consumption in the sweetening process, has reduced the desulfurization expense, has reduced the disposal cost of acid water simultaneously.
The capital equipment that the inventive method is used comprises: flue gas-ammonia blender, catalytic reduction reactor, heat exchanger, revolving bed absorption tower, the reverse contact tower of flue gas-alkali lye, H 2S stripping tower and demister etc.Other content in the inventive method can be confirmed by the conventional method in this area.
Through adopting above technical scheme, the following advantage of the acquisition of FCC technology of the present invention:
(1) to FCC flue gas not only denitration but also desulfurization.
(2) adopt the absorption equipment of rotary drill reactor as SOx, both reduced unit scale, improved absorption efficiency again, the absorption liquid acidity that obtains is higher, helps further utilization.
(3) because rotary drill reactor is the high efficient gas and liquid absorption equipment, the diluted acid amount that absorbs the SOx generation is little, can not roll up the processing water yield of acid water during acidifying acid water, can not improve processing cost.
That (4) has not only reduced FCC flue gas desulfurization adds the alkali cost, and has reduced the processing cost of acid water.
Description of drawings
Fig. 1 is the process unit flow chart of CN1895744A.
Fig. 2 is a process unit flow chart of the present invention.
Wherein: 1, FCC steam generator system; 2, supply the ammonia unit; 3, flue gas-ammonia blender; 4, catalytic reduction reactor; 5, heat exchanger; 6, deduster; 7, desulfurization unit; 8, chimney;
14, revolving bed absorption tower; 15, the reverse contact tower of flue gas-alkali lye; 16, demister; 18, diluted acid storage tank; 19, acid water storage tank; 20, acid solution-acid water blender; 21, heat exchanger; 22, H 2The S stripping tower; 23, settling tank; 24, divide flow container; 25, incinerator; 26, heat exchanger.
A-desulfurization absorption liquid; B-stripping air; The C-sediment; D-alkali lye; The E-water outlet drains into the sewage-farm.
The specific embodiment
Through specific embodiment FCC equipment for denitrifying flue gas of the present invention is elaborated below.Wherein gas phase is formed the percentage composition by volume, and liquid phase is formed percentage composition in mass.
Embodiment 1 (referring to Fig. 2)
From the flue gas of FCC steam generator system 1, air quantity 6m 3/ h, 300 ℃~400 ℃ of temperature contain 1000mg/m 3NO x, 1000mg/m 3SO 2, flue gas gets into flue gas-ammonia blender 4, mixes with the ammonia of confessing ammonia unit 2 at this flue gas full and uniformly, and (the ammonia consumption is NO in the flue gas to ammonia amount 6L/h xThe amount that complete reaction is required), gaseous mixture then gets into catalytic reduction reactor 4 downwards, and catalyst adopts and contains components such as V, Ti, W, the catalyst that reaction has good catalytic activity to SCR.
In beds, NO xAnd NH 3Reaction generates N 2And H 2O, the flue gas after the denitration of being come out by catalytic reduction reactor 4 gets into heat exchanger 5, and behind the recovery waste heat, flue gas is cooled to 80 ℃ by 340 ℃.Cooling back flue gas gets into revolving bed absorption tower 14.The dilute sulfuric acid that produces removes diluted acid storage tank 18.
The dilute sulfuric acid that comes out from diluted acid storage tank 18 gets into blender 20 to be mixed with acid water from acid water storage tank 19, and the acid-base neutralization reaction takes place, and mixed liquor is entering H after heat exchanger 21 is lowered the temperature 2S stripping tower 22 adopts an amount of air aeration, the H of effusion 2S gets into incinerator 25 and burns behind minute flow container 24.
From H 2S stripping tower 22 remove H 2The acid water of S gets into settling tank 23, removes incinerator after the head space gas that settling tank 23 produces also gets into branch flow container 24.
At acid water settling tank 23, after oxytropism water added adjusting PH with base>=7, part was as SO 2Absorption liquid goes to revolving bed absorption tower 14, and the remainder decontaminated water is handled the field.
The flue gas that comes out from revolving bed absorption tower 14 comprises FCC flue gas and incinerator smoke 2 parts, and the flue gas that comes out from revolving bed absorption tower 14 gets into the reverse contact tower 15 of flue gas-alkali lye, removes remaining SOx, the most laggard demister 16 demists, last smoke-input tube 8 dischargings.Flue NOx<10mg/m 3, SO 2<10mg/m 3, NH 3<5mg/m 3, produce dilute sulfuric acid 12L, concentration 0.1%~0.3%.
Embodiment 2 (referring to Fig. 2)
From the flue gas of FCC steam generator system 1, air quantity 100m 3/ h, 300 ℃~400 ℃ of temperature contain 500mg/m 3NO x, 2000mg/m 3SO 2, flue gas gets into flue gas-ammonia blender 4, mixes with the ammonia of confessing ammonia unit 2 at this flue gas full and uniformly, and (the ammonia consumption is NO in the flue gas to ammonia amount 50L/h xThe amount that complete reaction is required), gaseous mixture then gets into catalytic reduction reactor 4 downwards, and catalyst adopts and contains components such as V, Ti, W, the catalyst that reaction has good catalytic activity to SCR.
In beds, NO xAnd NH 3Reaction generates N 2And H 2O, the flue gas after the denitration of being come out by catalytic reduction reactor 12 gets into heat exchanger 5, and behind the recovery waste heat, flue gas is cooled to 70 ℃ by 340 ℃.Cooling back flue gas gets into revolving bed absorption tower 14.The dilute sulfuric acid that produces removes diluted acid storage tank 18.
The dilute sulfuric acid that comes out from diluted acid storage tank 18 gets into blender 20 to be mixed with acid water from acid water storage tank 19, and the acid-base neutralization reaction takes place, and mixed liquor is entering H after heat exchanger 21 is lowered the temperature 2S stripping tower 22 adopts an amount of air aeration, the H of effusion 2S gets into incinerator 25 and burns behind minute flow container 24.
From H 2S stripping tower 22 remove H 2The acid water of S gets into settling tank 23, removes incinerator after the head space gas that settling tank 23 produces also gets into branch flow container 24.
At acid water settling tank 23, after oxytropism water added adjusting PH with base>=7, part was as SO 2Absorption liquid goes to revolving bed absorption tower 14, and the remainder decontaminated water is handled the field.
The flue gas that comes out from revolving bed absorption tower 14 comprises FCC flue gas and incinerator smoke 2 parts, and the flue gas that comes out from revolving bed absorption tower 14 gets into the reverse contact tower 15 of flue gas-alkali lye, removes remaining SOx, the most laggard demister 16 demists, last smoke-input tube 8 dischargings.Flue NOx<10mg/m 3, SO 210mg/m 3, NH 3<5mg/m 3, produce dilute sulfuric acid 0.2m 3, concentration 0.1%~0.5%.
Embodiment 3 (referring to Fig. 2)
From the flue gas of FCC steam generator system 1, air quantity 2000m 3/ h, 300 ℃~400 ℃ of temperature contain 500mg/m 3NO x, 2000mg/m 3SO 2, flue gas gets into flue gas-ammonia blender 4, mixes with the ammonia of confessing ammonia unit 2 at this flue gas full and uniformly, and (the ammonia consumption is NO in the flue gas to ammonia amount 100L/h xThe amount that complete reaction is required), gaseous mixture then gets into catalytic reduction reactor 4 downwards, and catalyst adopts and contains components such as V, Ti, W, the catalyst that reaction has good catalytic activity to SCR.
In beds, NO xAnd NH 3Reaction generates N 2And H 2O, the flue gas after the denitration of being come out by catalytic reduction reactor 4 gets into heat exchanger 5, and behind the recovery waste heat, flue gas is cooled to 70 ℃ by 340 ℃.Cooling back flue gas gets into revolving bed absorption tower 14.The dilute sulfuric acid that produces removes diluted acid storage tank 18.
The dilute sulfuric acid that comes out from diluted acid storage tank 18 gets into blender 20 to be mixed with acid water from acid water storage tank 19, and the acid-base neutralization reaction takes place, and mixed liquor is entering H after heat exchanger 21 is lowered the temperature 2S stripping tower 22 adopts an amount of air aeration, the H of effusion 2S gets into incinerator 25 and burns behind minute flow container 24.
From H 2S stripping tower 22 remove H 2The acid water of S gets into settling tank 23, removes incinerator after the head space gas that settling tank 23 produces also gets into branch flow container 24.
At acid water settling tank 23, after oxytropism water added adjusting PH with base>=7, part was as SO 2Absorption liquid goes to revolving bed absorption tower 14, and the remainder decontaminated water is handled the field.
The flue gas that comes out from revolving bed absorption tower 14 comprises FCC flue gas and incinerator smoke 2 parts, and the flue gas that comes out from revolving bed absorption tower 14 gets into the reverse contact tower 15 of flue gas-alkali lye, removes remaining SOx, the most laggard demister 16 demists, last smoke-input tube 8 dischargings.Flue NOx<10mg/m 3, SO 2<10mg/m 3, NH 3<5mg/m 3, per season produces dilute sulfuric acid 4m 3, concentration 0.1%~3%.

Claims (6)

1. FCC flue gas managing technique method, comprise following content: the FCC flue gas at first mixes with ammonia, in the presence of catalyst, carries out the selective reduction denitration reaction of NOx then, it is characterized in that: the flue gas through the selective reduction denitration reaction adopts acid water to take off H 2Discharge water behind the S is that absorption liquid is rotated bed absorption desulfurization; The flue gas that revolving bed absorbs after the desulfurization further discharges after alkali lye absorbs desulfurization; Revolving bed absorbs the liquid phase of desulfurization discharge to be mixed with acid water, acid water pH value is adjusted to 4~6, and blows out H with air 2S, the H that blows out 2S goes incinerator to burn, and blows out H 2Sewage gets into the sewage-farm processing behind the S.
2. according to the described method of claim 1, it is characterized in that: the amount of the ammonia that mixes with the FCC flue gas is pressed 90%~110% of the required theoretical amount of NOx reduction reaction in the FCC flue gas and is confirmed.
3. according to the described method of claim 1, it is characterized in that: the flue gas after the denitration gets into the revolving bed absorption tower after heat exchanger heat exchange cooling, and absorption liquid adopts acid water to take off H 2Discharge water behind the S, the pH value of this discharge water is>=7.
4. according to the described method of claim 1, it is characterized in that: catalytic-reduction denitrified reaction temperature is 300 ℃~400 ℃.
5. according to the described method of claim 1, it is characterized in that: the liquid phase that revolving bed absorbs the desulfurization discharge is a dilute acid soln, and the diluted acid mass concentration is 0.1%~10%.
6. according to the described method of claim 1, it is characterized in that: air blows out H2S and obtains that the hydrogen sulfide volumetric concentration is 0.1%~3% in the gas.
CN2010102224121A 2010-07-07 2010-07-07 Fluid catalytic cracking (FCC) flue gas treatment method Pending CN102309910A (en)

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CN102600708A (en) * 2012-03-07 2012-07-25 杭州恒明环境技术有限公司 High-efficiency low-cost purification process of flue gas
CN102600708B (en) * 2012-03-07 2014-11-05 杭州恒明环境技术有限公司 High-efficiency low-cost purification process of flue gas
CN103285728A (en) * 2013-06-14 2013-09-11 中石化南京工程有限公司 Method and device for treating sulfur dioxide in sulfuric acid tail gas
CN103285728B (en) * 2013-06-14 2015-02-11 中石化南京工程有限公司 Method and device for treating sulfur dioxide in sulfuric acid tail gas
CN104258713A (en) * 2014-10-08 2015-01-07 美景(北京)环保科技有限公司 Acid gas treatment system and method based on ammonia-process desulfurization
CN104258713B (en) * 2014-10-08 2017-02-15 美景(北京)环保科技有限公司 Acid gas treatment system and method based on ammonia-process desulfurization
CN111644060A (en) * 2020-06-05 2020-09-11 中船澄西船舶修造有限公司 Marine smoke and dust processing apparatus
CN111701399A (en) * 2020-07-31 2020-09-25 中国石油化工股份有限公司 Method for treating volatile organic compounds of petrochemical enterprises
CN113108291A (en) * 2021-04-22 2021-07-13 红河州现代德远环境保护有限公司 Device for pretreating dichloroethane by pyrogenic process

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Application publication date: 20120111