CN106345250A - Ultralow emission process for catalytic cracking smoke - Google Patents

Ultralow emission process for catalytic cracking smoke Download PDF

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Publication number
CN106345250A
CN106345250A CN201610757773.3A CN201610757773A CN106345250A CN 106345250 A CN106345250 A CN 106345250A CN 201610757773 A CN201610757773 A CN 201610757773A CN 106345250 A CN106345250 A CN 106345250A
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China
Prior art keywords
flue gas
catalytic cracking
tower
minimum discharge
denitration
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CN201610757773.3A
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Chinese (zh)
Inventor
涂先红
陈卫红
裴旭东
李朝恒
郭荣群
张凡
郭玉涛
叶春波
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Sinopec Engineering Group Co Ltd
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Sinopec Engineering Group Co Ltd
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Priority to CN201610757773.3A priority Critical patent/CN106345250A/en
Publication of CN106345250A publication Critical patent/CN106345250A/en
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75Multi-step processes
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/14Separation 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 by absorption
    • B01D53/18Absorbing units; Liquid distributors therefor
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/60Simultaneously removing sulfur oxides and nitrogen oxides
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77Liquid phase processes
    • B01D53/78Liquid phase processes with gas-liquid contact
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/81Solid phase processes
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2251/00Reactants
    • B01D2251/10Oxidants
    • B01D2251/108Halogens or halogen compounds
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2251/00Reactants
    • B01D2251/30Alkali metal compounds
    • B01D2251/304Alkali metal compounds of sodium
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2251/00Reactants
    • B01D2251/50Inorganic acids
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2251/00Reactants
    • B01D2251/60Inorganic bases or salts
    • B01D2251/604Hydroxides
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2258/00Sources of waste gases
    • B01D2258/02Other waste gases
    • B01D2258/0283Flue gases
    • 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 provides an ultralow emission process for catalytic cracking smoke, comprising the following steps of: introducing an addition agent in a catalytic cracking catalyst, reducing Sox and NOx content in the catalytic smoke in a lower cost maximally, wherein the maximum concentration of NOx in the smoke does not exceed 400mg/m3; high temperature flue gas from a heat recovery boiler of a catalytic cracking device contacts with a circulation slurry in an urgent cooling desulfurizing tower to cool, dedust and desulfurize; the maximum concentration of the desulfurized smoke Sox does not exceed 150mg/m3; the desulfurized smoke enters the bottom ofa denitrating tower by a dustproof defroster to be in reverse contact with a denitrating solution; the denitrated smoke is evacuated after being removal of the fog; Soxin the smoke basically realizes zero emission; and when NOx content is below 30mg/Nm3, the purpose of ultralow emission is realized.

Description

A kind of catalytic cracking flue gas minimum discharge technique
Technical field
The present invention relates to chemical technology field, especially relate to a kind of catalytic cracking flue gas minimum discharge technique.
Background technology
Fcc (catalytic cracking) device is one of maximum pollutant emission source of oil plant, for meet environment protection control index and The requirement of emission reduction targets is it is necessary to strictly control the discharge capacity of catalytic cracking flue gas sox and nox.Current refinery controls catalytic cracking The Main Means of the noxious gas emissions such as flue gas sox, nox are that gas cleaning is processed.The fcc flue gas of domestic industrial applications takes off Sulfur technology has sodium alkali desulfurization, Regeneratable wet fuel gas desulfurizing, and denitration technology has scr denitration, ozone oxidation absorption process denitration.
Sodium alkali desulfurization is the most flue gas desulfurization techniques of current refinery fcc device application, removes in removing sox simultaneously Grain thing.Representative processes are the edv of duponttm belco company.But alkali method desulfurizing technology water consume and alkaline consumption are larger, saliferous is dirty The high outer discharge capacity of water concentration is big, and to the oil refining enterprise having strict drainage requirement, saline sewage needs to process further, this adds increased Construction investment and operating cost.
Regeneratable wet fuel gas desulfurizing technology is a kind of recovery so2Flue gas desulfurization technique, using organic amine absorbent, profit With the feature that absorbing agent absorption capacity is big, course of reaction is reversible, to so in flue gas2Carry out the chemical absorbing of high selectivity.Absorb so2Thermal regeneration isolates high-purity so to rich solution afterwards under certain condition2Gas is delivered to sulfur recovery unit and is produced sulfur, realizes Sulphur ressource recovery.Representative processes have the rasoc technique of sinopec, patent No. cn101185838a, this technique in Jinan branch company of petrochemical industry limited company has carried out commerical test.External shell company cansolv technique, the patent No. Cn1780678a, this technique has carried out commercial Application in Cangzhou branch company of sinopec limited company.But amine method takes off Sulfur technology rich solution regeneration steam consumption ratio is larger, and also ratio is larger for up-front investment, and in refinery's regenerated flue gas, sox content typically exists 800~1500mg/m3, for regenerable amine process desulfurization technology, concentration is relatively low, and economic benefit is inconspicuous, and this just limits Popularization and application in catalytic cracking unit for such technology.
Scr denitration technology is that a kind of flue gas that current domestic and international application is most, nox removal efficiency highest, technology are the most ripe takes off Nitre technology.Scr technique is to be 250~600 DEG C in temperature, with the amino such as ammonia or carbamide for reducing agent by nox under catalyst action SCR is converted into h2O and n2Process.Wherein with nh3- scr technology more mature and reliable.Scr technique is general It is divided into high temperature (450~600 DEG C) scr, middle temperature (320~450 DEG C) scr and low temperature (120~300 DEG C) scr.Scr denitration technology It has been successfully applied to catalytic cracking unit denitrating flue gas, the low problem of current low temperature scr catalyst sulfur resistive ability does not solve, So current catalytic cracking unit denitrating flue gas use middle temperature scr technology.The catalytic cracking unit that 20th century were designed is basic Do not reserve the position of equipment for denitrifying flue gas, and The Waste Heat Boiler of Catalytic Cracking Units exit gas temperature generally 180~230 DEG C, need denitration is partially placed in catalysis waste heat boiler, increased engineering construction difficulty, to catalysis waste heat boiler structure influence Larger.And this technological equipment investment is big, nh3Measure the actual presence controlling error of ratio with nox and cause NH_3 leakage, equipment corrosion etc. Problem.
Lower valency nitrogen oxides are insoluble in water, need to be carried out, with oxidant, the nitrogen oxides that nox is oxidized to high-valence state again Absorb.Representative processes have lotoxtm technique, and this technique is using ozone (o3) strong oxidizing property nox is oxidized to high-valence state Nitrogen oxides are absorbed with alkali liquor again.Lotoxtm technology at home and abroad has been enter into industrial applications stage, sinopec in 2013 Nanjing branch company of limited company applies this technology, but the preparation of ozone at this stage costly leads to operating cost higher. Ozone generator efficiency is low, power consumption is big, occupation of land is big, is likely to become the principal element of restriction lotoxtm Technique Popularizing.In theory It is 0.82kw h/kg o that ozone produces power consumption3, but during current typical commercial ozonator air source, power consumption is about 16kw·h/kg o3, with being about 6~8kw h/kg o during source of oxygen3.
Add auxiliary agent and can realize catalytic cracking flue gas desulphurization and denitration or simultaneous SO_2 and NO removal, the method does not need equipment Investment, using flexible, easy to operate, there are not potential liquid or solid waste disposal issues.Some states of USA and EU Family administers one of best techniques available using auxiliary agent is used as flue gas pollutant.Can be urged with reducing in certain limit using auxiliary agent Change sox, nox content in cracking flue gas, apply in general to the relatively low catalytic cracking unit of sox, nox content in flue gas.But Auxiliary agent method denitrification efficiency is low, unstable, poor to adaptability to raw material, catalysis flue gas in sox, nox content be difficult to simultaneously up to standard Discharge, and increase with fcc raw material in poor quality, the enforcement of new environmental regulation, sox, nox row up to standard simultaneously in catalysis flue gas Put and become more to be difficult to.
In view of this, the special proposition present invention.
Content of the invention
Object of the present invention is to provide a kind of catalytic cracking flue gas minimum discharge technique, described technique is with relatively low Cost achieves flue gas minimum discharge.
Inexpensive catalytic cracking flue gas minimum discharge technique, comprising:
Step s1, introduces auxiliary agent in catalytic cracking catalyst, reduces sox, nox content in catalysis flue gas to greatest extent Meanwhile, in flue gas nox maximum concentration no more than 400mg/m3
Step s2, connects in chilling desulfurizing tower and loop slurry from The Waste Heat Boiler of Catalytic Cracking Units high-temperature flue gas out Touch, carry out cooling down, dedusting, desulfurization, the flue gas sox maximum concentration after desulfurization is no more than 150mg/m3
Step s3, is entered denitrating tower bottom after the flue gas removing dust demister after desulfurization, is inversely contacted with denitration liquid, purifies Flue gas afterwards empties after mechanical demister, realizes the target of minimum discharge.
In step s1, described auxiliary agent is desulfurizing assistant agent or denitration auxiliary agent or simultaneous SO_2 and NO removal multiple-effect auxiliary agent.
Preferably, in step s2, described loop slurry is soda lye, and its ph value is 5~9.
Preferably, in step s2, described chilling desulfurizing tower is void tower.
Preferably, in step s3, described denitration liquid is containing chloritic alkaline solution, and its ph value is 7~13.
Preferably, in step s3, described denitration reaction tower can be void tower, packed tower, plate column or valve tower, preferentially Packed tower.
Preferably, in described denitration liquid, chloritic mass percent concentration is 0.01~10wt%.
When chlorite concentration is higher, denitrification efficiency is high, but corresponding cost also increases, and utilization rate reduces simultaneously, It is not suitable for industrial applications, be 0.1~10wt% chlorite and auxiliary combination after-purification effect from mass percent concentration More preferably, cost performance is higher, and more preferably mass percent concentration is 0.1~5wt%.
Preferably, also contain hypochlorite in described denitration liquid, it is weaker that hypochlorite compares chlorite oxidation's property, but with After chlorite compounds, its oxidisability is also stronger than single chlorite, and hypochlorite low cost, so adopt both Compositional liquor, can be with reduces cost it is ensured that while high removal efficiency, and preferred mass percent concentration is 0.01~10wt%, more Preferably 0.1~5wt%.
The ratio that hypochlorite and chlorite compound, that is, mol ratio be preferably 0.01~15, more preferably 0.1~8.
Preferably, response time during described denitration is 0.1~5 second, preferably 0.5~2 second.
Compared with prior art, the present invention is not only by multiple different purification process combination, but considers desulfurization comprehensively Denitration cost, sox removal efficiency, nox removal efficiency etc., reduce catalysis to greatest extent by the introducing relatively low cost of auxiliary agent and split While changing sox, nox content in flue gas, in preferential guarantee flue gas, nox maximum concentration is no more than 400mg/m3, by alkali cleaning Flue gas is carried out cool down, dedusting, desulfurization, the flue gas sox maximum concentration after desulfurization is no more than 150mg/m3, reduce follow-up as far as possible The consumption of denitration liquid, reduces desulphurization denitration cost, then removes flue fog drip and particulate matter further through dedusting demister, both Purify flue gas, decreased because flue gas carries the amount of the doctor solution entering denitrating tower secretly again, decrease the consumption of follow-up denitration liquid, Reduce denitration cost.Finally recycle chlorite to do oxidant and carry out deep desulfuration, denitration, the chlorous acid after advantageous embodiment Salt and the compositional liquor of hypochlorite, after purification, sulfureous in flue gas oxide concentration is substantially zeroed, and nox is 30mg/m3Hereinafter, reach super The target of low emission.
Compared with prior art, invention achieves following technique effect:
1. pass through to implement the present invention, the generation of pollutant in catalysis flue gas can be reduced from source, reduce follow-up flue gas Purification expense, reduces the outer discharge capacity of desulphurization denitration brine waste, can be with recovery section Sulphur ressource during auxiliary agent desulfurization.
2. pass through to implement the present invention, can be real in the case of not changing existing fcc device, not affecting the production of fcc device Existing flue gas desulfurization and denitrification, the shortcoming overcoming scr denitration technology.
3. pass through to implement the present invention, be capable of the ultra-clean discharge of flue gas: the sox in purifying smoke substantially realize zero-emission, Nox content controls in 30mg/nm3Below.
4. pass through to implement the present invention, denitration waste liquid can carry out oxidation processes as oxidant to desulfurization wastewater, on the one hand Denitration waste liquid has carried out secondary utilization, decreases efflux wastewater amount, on the other hand reduces desulfurization wastewater oxidation processes oxidant Consumption, and simplify operation.
Brief description
In order to be illustrated more clearly that the specific embodiment of the invention or technical scheme of the prior art, below will be to concrete In embodiment or description of the prior art the accompanying drawing of required use be briefly described it should be apparent that, below describe in Accompanying drawing is some embodiments of the present invention, for those of ordinary skill in the art, before not paying creative work Put, other accompanying drawings can also be obtained according to these accompanying drawings.
Fig. 1 is that a kind of catalytic cracking flue gas minimum discharge technique provided in an embodiment of the present invention takes off from flue gas through auxiliary agent desulfurization Schematic flow sheet after nitre.
Reference:
1- chilling desulfurizing tower, 2- dedusting demister, 3- denitrating tower, 4- machinery demister, 5- fresh water, 6- desulphurization circulating Serosity, 7- high-temperature flue gas, 8- desulfurization wastewater, 9- fresh soda, 10- denitration circulation fluid, the fresh denitration liquid of 11-, 12- denitration waste liquid, 13- purifying smoke.
Specific embodiment
Below in conjunction with the drawings and specific embodiments, technical scheme is clearly and completely described, but It is it will be understood to those of skill in the art that following described embodiment is a part of embodiment of the present invention rather than whole Embodiment, is merely to illustrate the present invention, and is not construed as limiting the scope of the present invention.Based on the embodiment in the present invention, ability The every other embodiment that domain those of ordinary skill is obtained under the premise of not making creative work, broadly falls into the present invention and protects The scope of shield.Unreceipted actual conditions person in embodiment, the condition according to normal condition or manufacturer's suggestion is carried out.Agents useful for same Or the unreceipted production firm person of instrument, being can be by the commercially available conventional products bought and obtain.
In describing the invention, it should be noted that term " " center ", " on ", D score, "left", "right", " vertical ", The orientation of instruction such as " level ", " interior ", " outward " or position relationship are based on orientation shown in the drawings or position relationship, merely to Be easy to describe the present invention and simplify description, rather than instruction or the hint device of indication or element must have specific orientation, With specific azimuth configuration and operation, therefore it is not considered as limiting the invention.Additionally, term " first ", " second ", " the 3rd " is only used for describing purpose, and it is not intended that indicating or hint relative importance.
In describing the invention, it should be noted that unless otherwise clearly defined and limited, term " installation ", " phase Even ", " connection " should be interpreted broadly, for example, it may be being fixedly connected or being detachably connected, or is integrally connected;Can To be to be mechanically connected or electrical connection;Can be to be joined directly together it is also possible to be indirectly connected to by intermediary, Ke Yishi The connection of two element internals.For the ordinary skill in the art, above-mentioned term can be understood at this with concrete condition Concrete meaning in invention.
Fig. 1 is that a kind of catalytic cracking flue gas minimum discharge technique provided in an embodiment of the present invention takes off from flue gas through auxiliary agent desulfurization Schematic flow sheet after nitre;As shown in figure 1, the present embodiment provide from flue gas after auxiliary agent desulphurization denitration catalytic cracking flue gas Purify technique, comprising:
From The Waste Heat Boiler of Catalytic Cracking Units, out the high-temperature flue gas 7 after auxiliary agent desulphurization denitration enter chilling desulfurizing tower 1, Contact with desulphurization circulating serosity 6, carry out cooling down, dedusting, desulfurization, be 5~9 by adding fresh soda 9 to control serosity ph value, pass through Supplement fresh water 5 and maintain water balance in tower, simultaneously outer row's desulfurization waste liquor 8, from chilling desulfurizing tower 1 flue gas removing dust demisting out Enter denitrating tower 3 bottom after device 2, inversely contact with denitration circulation fluid 10, carry out deep desulfuration, denitration, according to purifying smoke 13 Middle nox concentration supplements fresh denitration liquid 11, and denitration waste liquid 12 is constantly outer simultaneously arranges, and the flue gas after denitration is after mechanical demister 4 Emptying.
Embodiment 1
The first step: auxiliary agent desulphurization denitration
In flue gas before certain refinery catalytic cracking flue gas adding assistant, nox, sox content is respectively 1360mg/m3、200mg/m3, plus Enter to account for the denitration auxiliary agent (ldn-1 denitration auxiliary agent) of catalytic cracking catalyst general reserve 1.5%, stable rear demarcation, catalysis is split Change nox, sox content in flue gas and be respectively 340mg/m3、180mg/m3, denitration rate is 75%.
Second step: desulfurization
It is fully contacted with loop slurry in chilling scrubbing tower from fcc device by utilizing waste heat boiler flue gas out, by adding Fresh soda lye, controls loop slurry ph value to be 5~9.Chilling scrubbing tower is void tower.SO 2 from fume concentration after purification is 30mg/m3, desulfurization degree is 83.3%.
3rd step: denitration
Enter denitration tower bottom from desulfurizing tower flue gas out to be inversely fully contacted with denitration liquid, denitrating tower is packed tower. It is absorbent using sodium chlorite solution, its mass fraction is 4%.Absorb temperature and be 50 DEG C, the time of staying is 1s, liquid-gas ratio is 0.5l/m3.After counter current contacting, sox, nox are substantially oxidized absorption, and sulfur dioxide in flue gas concentration is substantially zeroed, in flue gas Nox concentration is down to 30mg/m3.
Embodiment 2
The first step: auxiliary agent desulphurization denitration
In flue gas before certain refinery catalytic cracking flue gas adding assistant, nox, sox content is respectively 100mg/m3、1115mg/m3, plus Enter to account for the desulfurizing assistant agent (lst-1 desulfurizing assistant agent) of catalytic cracking catalyst general reserve 4%, stable rear demarcation, catalytic cracking In flue gas, nox, sox content is respectively 95mg/m3、245mg/m3, desulfurization degree is 78%.
Second step: desulfurization
It is fully contacted with loop slurry in chilling scrubbing tower from fcc device by utilizing waste heat boiler high-temperature flue gas out, pass through Add fresh soda lye, control loop slurry ph value to be 5~9.Chilling scrubbing tower is void tower.SO 2 from fume after purification is dense Spend for 29.5mg/m3, desulfurization degree is 88%.
3rd step: denitration
Enter denitration tower bottom from desulfurizing tower flue gas out to be inversely fully contacted with denitration liquid, denitrating tower is packed tower. It is absorbent using sodium chlorite solution, its mass fraction is 1.5%.Absorb temperature and be 50 DEG C, the time of staying is 1s, liquid-gas ratio For 0.4l/m3.After counter current contacting, sox, nox are substantially oxidized absorption, and sulfur dioxide in flue gas concentration is substantially zeroed, flue gas Middle nox concentration is down to 15mg/m3.
Embodiment 3
The first step: auxiliary agent desulphurization denitration
In flue gas before certain refinery catalytic cracking flue gas adding assistant, nox, sox content is respectively 260mg/m3、935mg/m3, plus Enter to account for the multiple-effect auxiliary agent (lta-1 multiple-effect auxiliary agent) of catalytic cracking catalyst general reserve 2.5%, stable rear demarcation, catalysis is split Change nox, sox content in flue gas and be respectively 158mg/m3、290mg/m3, denitration rate is 39.2%, and desulfurization degree is 68.9%.
Second step: desulfurization
It is fully contacted with loop slurry in chilling scrubbing tower from fcc device by utilizing waste heat boiler flue gas out, by adding Fresh soda lye, controls loop slurry ph value to be 5~9.Chilling scrubbing tower is void tower.SO 2 from fume concentration after purification is 42mg/m3, desulfurization degree is 85.5%.
3rd step: denitration
Enter denitration tower bottom from desulfurizing tower flue gas out to be inversely fully contacted with denitration liquid, denitrating tower is packed tower. Temperature be 50 DEG C, liquid-gas ratio be 0.3l/m3, denitration liquid naclo2When mass concentration is 2.5%, time of staying 1.1s, sox, Nox is substantially oxidized absorption, and after denitration, sulfur dioxide in flue gas concentration is substantially zeroed, and nox is 25mg/m3.
Embodiment 4
Difference with embodiment 3 is naclo during denitration2Mass percent concentration is 10%.
After denitration, sulfur dioxide in flue gas concentration is substantially zeroed, and nox is 5mg/m3Below.
Embodiment 5
Difference with embodiment 3 is that denitration liquid during denitration is naclo2With the mixed liquor of naclo, when naclo with naclo2When mol ratio is 1.2:1, after denitration, sulfur dioxide in flue gas concentration is substantially zeroed, and nox is 10mg/m3.
Finally it is noted that various embodiments above, only in order to technical scheme to be described, is not intended to limit;To the greatest extent Pipe has been described in detail to the present invention with reference to foregoing embodiments, it will be understood by those within the art that: its according to So the technical scheme described in foregoing embodiments can be modified, or wherein some or all of technical characteristic is entered Row equivalent;And these modifications or replacement, do not make the essence of appropriate technical solution depart from various embodiments of the present invention technology The scope of scheme.

Claims (10)

1. a kind of catalytic cracking flue gas minimum discharge technique is it is characterised in that include:
Step s1, introduces auxiliary agent in catalytic cracking catalyst, while reducing sox, nox content in catalysis flue gas, in flue gas Nox concentration is less than 400mg/m3
Step s2, from described The Waste Heat Boiler of Catalytic Cracking Units high-temperature flue gas out in chilling desulfurizing tower and desulphurization circulating serosity Contact, carry out cooling down, dedusting, desulfurization, the flue gas sox concentration after desulfurization is less than 150mg/m3
Step s3, is entered denitrating tower bottom after the flue gas removing dust demister after described desulfurization, is inversely contacted with denitration liquid, purifies Flue gas afterwards empties after mechanical demister, realizes the target of minimum discharge.
2. catalytic cracking flue gas minimum discharge technique according to claim 1 it is characterised in that:
In step s1, described auxiliary agent is the multiple-effect auxiliary agent of single auxiliary agent or simultaneous SO_2 and NO removal;Described single auxiliary agent is desulfurization Auxiliary agent or denitration auxiliary agent.
3. catalytic cracking flue gas minimum discharge technique according to claim 1 it is characterised in that:
In step s2, described loop slurry is soda lye, and its ph value is 5~9.
4. catalytic cracking flue gas minimum discharge technique according to claim 1 it is characterised in that:
In step s3, described denitration liquid is containing chloritic alkaline solution, and its ph value is 7~13, and mass percent is dense Spend for 0.1~10wt%, preferably 0.1~5wt%.
5. catalytic cracking flue gas minimum discharge technique according to claim 4 it is characterised in that:
Hypochlorite is also contained, mass percent concentration is 0.1~10wt%, preferably 0.1~5wt% in described denitration liquid.
6. catalytic cracking flue gas minimum discharge technique according to claim 5 it is characterised in that:
In described denitration liquid, hypochlorite and chloritic mol ratio are 0.01~15, preferably 0.01~8.
7. catalytic cracking flue gas minimum discharge technique according to claim 1 it is characterised in that:
Response time during described denitration is 0.1~5 second, preferably 0.5~2 second.
8. catalytic cracking flue gas minimum discharge technique according to claim 1 it is characterised in that:
In step s2, described chilling desulfurizing tower is void tower.
9. catalytic cracking flue gas minimum discharge technique according to claim 1 it is characterised in that:
In step s3, described denitrating tower is packed tower, plate column or void tower, preferred filler tower.
10. catalytic cracking flue gas minimum discharge technique according to claim 1 it is characterised in that:
In step s3, in the flue gas after described purification, sox realizes zero-emission, nox content in 30mg/nm3Below.
CN201610757773.3A 2016-08-29 2016-08-29 Ultralow emission process for catalytic cracking smoke Pending CN106345250A (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
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Application publication date: 20170125