CN102397784B - Method for regenerating flue gas desulphurization and denitrification adsorbent by hydrogen sulfide-containing regeneration gas - Google Patents
Method for regenerating flue gas desulphurization and denitrification adsorbent by hydrogen sulfide-containing regeneration gas Download PDFInfo
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Abstract
The invention discloses a method for regenerating a flue gas desulphurization and denitrification adsorbent by hydrogen sulfide-containing regeneration gas. The method comprises the following steps that an adsorbent is introduced into a flue gas absorber and contacts with catalytic cracking catalyst-regenerated flue gas so that sulfides and nitrides in the catalytic cracking catalyst-regenerated flue gas is removed by adsorption; the adsorbent which adsorbs the sulfides and/or the nitrides and needs to be regenerated is introduced into an adsorbent regenerator; and hydrogen sulfide-containingreduction gas is subjected to preheating and heating, then is fed into the adsorbent regenerator and contacts the adsorbent needing to be regenerated to undergo a desorption regeneration reaction at a high temperature. The method provided by the invention utilizes hydrogen sulfide as a reduction gas ingredient and hydrogen sulfide can directly undergo an oxidation reduction reaction with a flue gas desulphurization and denitrification adsorbent. In addition, the method adopts a reduction gas circulation mode and realizes integrated utilization of heat of high-temperature regenerated tail gas and a regenerant.
Description
Technical field
The present invention relates to the renovation process in a kind of hydrocarbon oil catalytic cracking process, more particularly, relate to the renovation process of regeneration flue gas desulfurization denitrification adsorbent in a kind of catalytic cracking unit.
Background technology
Catalytic cracking catalyst circulates between reactor and regenerator, when leaving reactor, contains the about 3～10wt% of coke on the catalyst usually, and the coke that must deposit with airborne oxygen burning-off in regenerator is to recover catalytic activity.The coke that deposits on the catalyst mainly is reaction condensate, and main component is carbon and hydrogen, when cracked stock sulfur-bearing and nitrogen, also contains sulphur and nitrogen in the coke.Catalyst warp and the oxygen of carbon deposit carry out regenerative response, generate CO
2, CO and H
2O also contains SOx (SO in the regenerated flue gas
2, SO
3) and NOx (NO, NO
2).Regenerative response is exothermic reaction, and fuel factor is quite big, and the heat that provides this device thermal balance required is provided.
To handling the pollution problem of industrial smoke sulphur oxide and nitrogen oxide, people such as Asit K.Das disclose a kind of method that removes oxysulfide and nitrogen oxide simultaneously, SO
2-NO
xAdsorption process, namely the SNAP method is (referring to " Simultaneous Adsorption of SO
2-NOx from Flue Gases in a Riser Configuration ", people such as Asit K.Das, AIChE Journal, Vol.47, No.12, December 2001, P2831-2844).This method makes flue gas and the Na/ γ-Al that contains oxysulfide and nitrogen oxide
2O
3The adsorbent contact, this adsorbent can adsorb oxysulfide and nitrogen oxide, thereby reaches the purpose that purifies flue gas.Described contact can be carried out in gas suspension absorber (GSA), and the temperature of contact is that 100～150 ℃, time of contact are 5 seconds.After contact was finished, the absorbent particles that is adsorbed with oxysulfide and nitrogen oxide was collected with filter bag.Na/ γ-Al after the SNAP method is used
2O
3Adsorbent can be regenerated.Na/ γ-Al
2O
3The regenerative process of adsorbent is divided two stages: the adsorbent after (1) will use in the fluidized bed type regenerator is heated to 500 ℃, discharges NO
xFeed natural gas subsequently with NO
xBe reduced to N
2And O
2Discharging; (2) will remove NO in (1)
xAdsorbent again through natural gas and steam treatment with SO
xBe converted into H
2S reclaims.
CN101209391A discloses a kind of method and cracking method for hydrocarbon oil that removes flue gas sulphur oxide and/or nitrogen oxide, adopt catalytic cracking catalyst as the adsorbent that removes catalytic cracking catalyst regenerated flue gas sulphur oxide and nitrogen oxide in this method, its adsorption effect is suitable with existing special-purpose adsorbent, and be not easy saturated, the condition of adsorbent reactivation is (such as being heated to 500 ℃, release NOx) condition that likens to catalytic cracking catalyst regeneration relaxes, therefore as the structure not influence of adsorbent reactivation to catalytic cracking catalyst, in addition, handle the used catalyst of adsorbent as regeneration fume from catalytic cracking, still can use in the catalytic cracking process, its activity as catalytic cracking catalyst is not only unaffected, and slightly improves.
Utilize the adsorbent oxysulfide in the adsorbing and removing regenerated flue gas and nitrogen oxide before flue gas emptying, adsorption temp (being flue-gas temperature) is generally about 200 ℃.The processing of can regenerating of adsorbent to be generated after the absorption, temperature is 500～600 ℃ during regeneration; Adsorbent after the regeneration can turn back in the flue gas adsorptive reactor and reuse.Regenerative operation is in reducing atmosphere, and reducibility gas derives from the dry gas of oil plant, and is preferably selected from hydrogen, carbon monoxide, methane, ethane, propane, butane, pentane and the various isomers thereof one or more.
Reducibility gas in the adsorbent reactivation device under the high temperature with spent agent on sulfate, sulphite, nitrate, nitrite etc. redox reaction takes place, generate elemental sulfur, hydrogen sulfide, carbon dioxide, water etc., typical reaction is with reference to following (be example with the divalent metal M):
MSO
4+3H
2＝MO+S+3H
2O (1)
S+H
2＝H
2S (2)
MSO
4+4H
2＝MS+4H
2O (3)
MS+3MSO
4＝4MO+4SO
2 (4)
MSO
3＝MO+SO
2 (5)
SO
2+2H
2＝S+2H
2O (6)
M(NO
3)
2+5H
2＝N
2+MO+5H
2O (7)
Hydro carbons+MSO
4→ MCO
3+ H
2S+H
2O+S+CO
2(8)
When implementing the adsorbent reactivation operation, owing to be subjected to the influence of factors such as mass transfer between the gas-solid, the reducing gases consumption will cause the effective rate of utilization of reducing gases to reduce much larger than the required theoretical consumption of regeneration spent agent.
On the other hand, the dry gas of oil plant all contains hydrogen sulfide as the dry gas of catalytic cracking unit, the tail gas of hydrocracking unit etc.Usually before dry gas is utilized, all to through the operating unit that removing hydrogen sulfide earlier.
Summary of the invention
The technical problem that the present invention solves provides the method for utilizing hydrogen sulfide containing reducing gas regeneration flue gas desulfurization denitrification adsorbent and the method that fully utilizes the high temperature regeneration tail gas heat quantity.
The renovation process of the hydrogen sulfide containing flue gas desulfuration and denitrification adsorbent of a kind of regeneration gas provided by the invention comprises adsorbent is introduced in the flue gas absorber, contacts the sulphur in the adsorbing and removing flue gas, nitride with the catalytic cracking catalyst regenerated flue gas; Will adsorb the adsorbent to be generated of sulfide and/or nitride introduce in the adsorbent reactivation device, reducing gas is introduced in the adsorbent reactivation device, contact with adsorbent to be generated and carries out desorption and regeneration and react under higher temperature; Contain hydrogen sulfide in the described reducing gas.
The beneficial effect of method provided by the invention is:
The sulphur and the nitrogen that utilize hydrogen sulfide containing reducing gas will be adsorbed on the adsorbent are converted into elemental sulfur and gaseous nitrogen atmosphere, and regeneration effect is better; Simultaneously reducing gas can directly recycle without removing hydrogen sulfide, adopts the reducing gas that contains hydrogen sulfide, can directly use in the refinery hydrogen sulfide containing gases such as dry gas, does not need to have shortened flow process through removing the step of hydrogen sulfide.In addition, hydrogen sulfide also is a kind of better reductant, and its utilization can be saved the consumption of other class reducing agent, has improved the utilization rate of reducing gas.
Description of drawings
Accompanying drawing is the renovation process schematic flow sheet of flue gas desulfuration and denitrification adsorbent provided by the invention.
Wherein: A-flue gas absorber; B-adsorbent reactivation device; C-regenerative agent heat exchanger; D-spent agent preheater; E-regeneration gas heater; The F-heat exchanger; The G-cooler; The H-compressor.The 1-smoke inlet; 2-purifies exhanst gas outlet; 3-sorbent circulation pipe; 4,6-inclined tube; 5-spent agent riser; 7,8-unloads the agent pipeline; 9-adds the agent pipeline; The fresh reducing gas of 10-; 11-14,15,17,18-control valve; The 12-spent agent promotes gas; 13-circulation reducing gases; The 16-regeneration tail gas; 19-returns the reducing gases of gas pipe network
The specific embodiment
The hydrogen sulfide containing flue gas desulfuration and denitrification adsorbent renovation process of regeneration gas provided by the invention is so concrete enforcement:
The renovation process of flue gas desulfuration and denitrification adsorbent provided by the invention, flue gas desulfuration and denitrification adsorbent adsorbent (abbreviation adsorbent) is introduced in the flue gas absorber, contact with the catalytic cracking catalyst regenerated flue gas, sulphur in the adsorbing and removing flue gas, nitride, described flue gas absorber is fluidized-bed reactor, wherein, the filling density of adsorbent is 0.01～200kg/m
3, preferred 0.5～120kg/m
3, the operating temperature in the flue gas absorber is 50～400 ℃, preferred 100～300 ℃; Pressure is 0.001～0.20MPa, preferred 0.005～0.15MPa.
In the method provided by the invention, the adsorbent to be generated that has adsorbed sulfide and/or nitride is introduced in the adsorbent reactivation device, hydrogen sulfide containing reducibility gas enters in the adsorbent reactivation device through preheating, contacts with adsorbent to be generated and carry out desorption and regeneration under higher temperature.The filling density of adsorbent mixtures to be generated is 2～300kg/m in the described absorption regeneration device
3, preferred 20～250kg/m
3Operating temperature in the absorption regeneration device is 450～650 ℃, and operating pressure is 0.005～0.60MPa, preferred 0.01～0.40MPa.
Preferred scheme is that reducing gas enters the adsorbent reactivation device before at first through after the heater heating, and temperature reaches 700～850 ℃, then enters the adsorbent reactivation device, directly heats and the adsorbent to be generated of regenerating.
In the method provided by the invention, preferred scheme is that 50～400 ℃ adsorbent to be generated is by after drawing in the flue gas absorber with having adsorbed oxysulfide and/or nitrogen oxide, temperature, enter before the adsorbent reactivation device, enter as cooling medium and carry out preheating in the preheater; Cooling medium rises through heat exchanger by promoting air lift, reaches 300～400 ℃ after the heat exchange.Suitable in the oil plant, hot logistics easily that the heat carrier of described heat exchanger can be taken from is as the hot logistics in catalytic cracking unit itself or the flue gas adsorption-regeneration system.
In the method provided by the invention, reducing gas in contain hydrogen sulfide, the volumn concentration of hydrogen sulfide is 0.5%-80%, preferred 0.5%-20%.The combined feed flow rate of reducing gas is determined with reference to the concentration of raw material sulphur oxide, nitrogen oxide, does excessive processing generally speaking, get theoretical consumption 2～20 times, is preferably 3～12 times.
Reducibility gas in the adsorbent reactivation device under high temperature with spent agent on sulfate, sulphite, nitrate, nitrite etc. except the reaction that (1)～(8) take place, when containing hydrogen sulfide, also following reaction can take place:
SO
2+2H
2S＝3S+2H
2O (9)
MSO
4+3H
2S＝MO+4S+3H
2O (10)
M(NO
3)
2+5H
2S＝N
2+MO+5S+5H
2O (11)
Contain the elemental sulfur that responds and generate in the regeneration tail gas, need cooling to reclaim.Regeneration tail gas own cooling when entering in the heat exchanger the cold reducing gas of preheating after the conventional dedusting separated out elemental sulfur, and compressed machine returns in the regenerator or enters refinery's gas pipe network afterwards; The all or part of heat exchange of the adsorbent after the regeneration is returned in the flue gas absorber and is used after cooling, also can be by carrying gas to turn back in the catalytic cracking catalyst regenerator or in the catalyst cracker.
In the method provided by the invention, described adsorbent be catalytic cracking catalyst or with the Solid-state Chemistry agent of catalytic cracking unit compatibility.
In the method provided by the invention, described flue gas adsorbent is catalytic cracking catalyst, can be in the constituent of fresh catalytic cracking catalyst, catalytic cracking catalyst to be generated, regeneration catalyzing Cracking catalyst and above-mentioned catalyst one or more.After introducing the regeneration of adsorbent reactivation device, the saturated adsorbent of at least part of absorption returns the flue gas absorber.
In the method provided by the invention, one or more in the described reduction air-flow that enters the adsorbent reactivation device in containing hydrogen, carbon monoxide, methane, ethane, propane, butane, pentane and various isomers thereof,
In the method provided by the invention, described reducing gas preferably uses the dry gas in the oil plant, be selected from catalytic cracking tail gas, catalytic reforming tail gas, hydrocracking tail gas and the delayed coking tail gas one or more, wherein allow to exist hydrogen sulfide, namely through removing the air-flow of hydrogen sulfide treatment.
In the method provided by the invention, contain elemental sulfur in the regeneration tail gas, need cooling to reclaim.Regeneration tail gas is through entering in the first-class heat exchanger after the conventional dedusting, and this moment, heat side was regeneration tail gas, and temperature is the cold reducing gas from compressor outlet at 450～650 ℃, cold side, and temperature is at 35～120 ℃.In first-class heat exchanger, hot side's gas is cooled to 170～300 ℃, can condensation separate out the part elemental sulfur, enters secondary condenser afterwards; Cold side is heated to 200～300 ℃, enters afterwards to enter regenerator after regeneration gas heaters heats.In secondary condenser, the hot gas that is entrained with elemental sulfur is cooled to 30～40 ℃, and elemental sulfur is separated out fully, and the entrance that has also satisfied compressor simultaneously requires temperature.Behind the reducing gas of compressor suction from secondary condenser, outlet at first has two big whereabouts: when concentration of hydrogen sulfide in the reducing gases surpasses 5%, with reducing gases compression and back gas pipe network, replenish fresh reducing gas to system simultaneously; Otherwise compressor is circulated back to regenerative system with reducing gas, and be divided into two-way this moment again, and wherein one road gas at first enters the preheating of regenerative agent heat exchanger as the lifting gas of spent agent; Another road gas enters the first-class heat exchanger preheating as reducing gases.
In the method provided by the invention, preferred scheme is that 50～400 ℃ adsorbent to be generated is by after drawing in the flue gas absorber with having adsorbed oxysulfide and/or nitrogen oxide, temperature, enter before the adsorbent reactivation device, enter as cooling medium and carry out preheating in the preheater; Cooling medium rises through heat exchanger by promoting air lift, reaches 300～400 ℃ after the heat exchange.Suitable in the oil plant, hot logistics easily that the heat carrier of described heat exchanger can be taken from is as the hot logistics in catalytic cracking unit itself or the flue gas adsorption-regeneration system.
Described lift gas is the mixture of reducibility gas, inert gas or reducibility gas and inert gas.Described reducibility gas is the part of compressor outlet gas; Described inert gas is selected from one or more in zero group gas, nitrogen, carbon dioxide and the water vapour in the periodic table of elements.Be preferably the reducibility gas identical with entering the regenerator composition.
In the method provided by the invention, preferred scheme is that lift gas enters preheating in the reproducing adsorbent heat exchanger, and cold logistics is reduction air-flow and air, and hot logistics is that the temperature of drawing in the adsorbent reactivation device is 500～650 ℃ reproducing adsorbent.After the heat exchange, 150～300 ℃ in reduction air-flow, hot logistics is cooled to 200～300 ℃.
Described regenerative agent heat exchanger is the heat-exchanger rig that contains tube side and shell side, and tube side can be single tube, also can be shell and tube.Heat carrier can select heat carrier to walk tube side with the operation of fluidisation attitude, and cooling medium is walked shell side, also can select heat carrier to walk shell side, and cooling medium is walked tube side.Preferred heat carrier is walked tube side, and cooling medium is walked shell side.
In the method provided by the invention, all or part of heat exchange of the adsorbent after the regeneration is returned in the flue gas absorber and is used after cooling, also can be by carrying gas to turn back in the catalytic cracking catalyst regenerator or in the catalyst cracker.
The preferred scheme of the present invention be hydrogen sulfide as one of regeneration reducing source of the gas, condenser is set reclaims simple substance on the one hand and satisfy the compressor instructions for use on the other hand, reduced the severity to the reducing gas source, improved the utilization rate to reducing gas again.
Specify the specific embodiment of method provided by the invention with reference to the accompanying drawings, but therefore the present invention is not restricted:
As shown in drawings, adsorbent is packed among the flue gas absorber A by adding agent mouth 9, pending flue gas is fed among the flue gas absorber A by entrance 1, adsorbent contacts with regenerated flue gas, oxysulfide in the adsorbing and removing flue gas and/or nitrogen oxide, the tail gas after the purification takes off dirt discharge flue gas absorber from purifying exhanst gas outlet 2 through routine.Adsorbent to be generated after the use is by inclined tube 4 output flue gas absorbers, and the adsorbent after a part is used still has certain adsorption capacity, can return among the flue gas absorber A by sorbent circulation pipe 3 to reuse.
Be input to adsorbent to be generated among the spent agent heat exchanger D through inclined tube 4, nationality enters heat exchanger D by promoting the castering action that gas entrance 12 introduces gases along pipeline 5, and spent agent enters adsorbent reactivation device B after heat exchange promotes temperature.
Can draw the adsorbent of adsorption system through unloading agent mouth 7.
In adsorbent reactivation device B, adsorbent to be generated contacts regeneration with high temperature reduction gas; When adsorbent was catalytic cracking catalyst, one of flow direction of reproducing adsorbent was all or part of through unloading the reactor of agent mouth 8 introducing catalytic cracking regenerators or catalytic cracking unit; Two of the flow direction of reproducing adsorbent is to enter regenerative agent heat exchanger C and cold reducing gases logistics 12 heat exchange through inclined tube 6, returns afterwards among the absorber A.
Fresh reducing gas is through entrance 10, and the switch by valve 11 and valve 17 fits into the reducing gas pipeline, and be divided into 12 and 13 two-way afterwards: 12 is that spent agent promotes gas, through entering the spent agent lift line after the regenerative agent heat exchanger C preheating; 13 is the regenerator reducing gas, enters among the regenerator D after reducing gases heater E heats up through entering after the first-stage condenser F preheating, finishes the regeneration purpose.
The regeneration tail gas of being made up of reducing gases and lifting gas enters pipeline 16 through after the conventional dedusting, enters first-stage condenser F cooling afterwards, reclaims a part of elemental sulfur; Then gas enters among the secondary coolers G and cools off, and enters compressor H afterwards.
Behind the reducing gas of compressor suction from secondary condenser H, outlet has two selection: the one, and by the cooperation of valve 17 and valve 18, through pipeline 19 compression and back gas pipe networks, replenish fresh reducing gas by valve 11 and pipeline 10 to system this moment with reducing gas; The 2nd, by driving valve 17, pass valve 11 and valve 18 compressors reducing gas is circulated back to regenerative system, be divided into two-way this moment again, and wherein one road gas 12 at first enters the preheating of regenerative agent heat exchanger as the lifting gas of spent agent; Another road gas 13 enters the first-class heat exchanger preheating as reducing gases.
Further specify method provided by the invention below by embodiment, but therefore the present invention is not subjected to any restriction.
Comparative Examples
The second adsorption performance of the adsorbent after the explanation of this Comparative Examples is regenerated by not hydrogen sulfide containing reducing gas.
1, adsorbent reactivation to be generated
Adsorbent adopts conventional MLC-500 fresh catalyst (Qilu Petrochemical company catalyst plant is produced).Sulfide and the nitride in the absorption flue gas in the flue gas absorber of at first adsorbent being packed into, then the adsorbent to be generated of inactivation is packed in the adsorbent reactivation device, described adsorbent reactivation device is that fixed fluidized bed (quartz ampoule, live part Φ 32mm * 600mm), dress dosage is 25g.Reducing gas being fed to be generated adsorbent bed, is that reducing gas contacts 20min with adsorbent to be generated under the condition of 20h-1 at 600 ℃, normal pressure, weight (hourly) space velocity (WHSV).The percentage by volume of hydrogen is 30% in the described reducing gas, and all the other are balance gas argon.Adopt raw material and the tail gas (comprising hydrogen sulfide) of Agilent3000A on-line analysis regenerative process, in regeneration tail gas, detected the hydrogen sulfide of 157ppm through chromatogram, hydrogen capacity in the regeneration gas or even excessive is described.Adsorbent to be generated is reduced regeneration and recovers active.
2, regeneration recovery hypersober carries out second adsorption
Flue gas fed be equipped with in the said fixing fluidized-bed adsorber of adsorbent, the described adsorbent adsorbent after the not hydrogen sulfide containing reducing gas regeneration of serving as reasons, adding dosage is 25g.At 200 ℃, normal pressure, weight (hourly) space velocity (WHSV) 100h
-1Condition under flue gas contact with adsorbent.Adopt flue gas and the tail gas of the comprehensive flue gas analyzer on-line analysis of KM9106 type adsorption process.The composition of flue gas sees Table 1.
When carrying out adsorption operations, to the removal efficiency (X of target contaminant
i) change procedure from high to low arranged, as by initial near 100% finally about 60%.General Definition is time of break-through to the removal efficiency of target contaminant low absorption duration of runs by 90% o'clock, is designated as t
st
sRepresent adsorbent and keep the ability of efficient running.The amount of the unit's of definition adsorbents adsorb target contaminant is adsorption capacity in addition, is designated as C
p, adsorption capacity is more big, and the performance of adsorbent is more strong.
The volume of table 1 flue gas is formed
| Component | H 2O | SO 2 | NO | NO 2 | CO 2 | O 2 | N 2 |
| Volume fraction, % | 10.0 | 0.1418 | 0.060 | 0.0038 | 13.95 | 2.61 | 73.26 |
Embodiment 1-6
The second adsorption performance of the adsorbent after embodiment 1-6 explanation is regenerated through the reducing gases of hydrogen and hydrogen sulfide.
Adsorbent regeneration method to be generated according to step 1 in the Comparative Examples 1, under keeping the constant prerequisite of other condition, in regeneration gas, add hydrogen sulfide, the volume fraction of hydrogen sulfide is respectively 0.5%, 1.0%, 1.5%, 2.5%, 5.0%, 10.0%, the total volume fraction of hydrogen sulfide and hydrogen is 30%, and surplus is balance gas argon gas.The second adsorption results of property of adsorbent sees Table 2.
Table 2, the second adsorption performance of the adsorbent after regeneration
By table 2 as seen, behind the adding hydrogen sulfide, the second adsorption performance of reproducing adsorbent is improved in the reducing gas, and the performance of especially adsorbing sulfur dioxide improves a lot.
Claims (9)
1. the renovation process of the hydrogen sulfide containing flue gas desulfuration and denitrification adsorbent of regeneration gas comprises adsorbent is introduced in the flue gas absorber, contacts the sulphur in the adsorbing and removing flue gas, nitride with the catalytic cracking catalyst regenerated flue gas; Will adsorb the adsorbent to be generated of sulfide and/or nitride introduce in the adsorbent reactivation device, reducing gas is introduced in the adsorbent reactivation device, contact with adsorbent to be generated and carries out desorption and regeneration and react under higher temperature; It is characterized in that containing in the described reducing gas hydrogen sulfide that volume fraction is 0.5%-80%, the temperature that described adsorbent to be generated enters before the adsorbent reactivation device is 300～400 ℃, and adsorbent reactivation device outlet temperature is 450～650 ℃.
2. according to the method for claim 1, the volume fraction that it is characterized in that hydrogen sulfide in the described reducing gas that enters in the regenerator is 0.5%-20%.
3. according to the method for claim 1, it is characterized in that described adsorbent to be generated is by after drawing in the flue gas absorber, before the introducing adsorbent reactivation device, introduce in the spent agent preheater as medium to be heated, and carry out heat exchange by the regeneration tail gas of drawing in the adsorbent reactivation device heating bath muff.
4. according to claim 1,2 or 3 method, it is characterized in that reproducing adsorbent is drawn by the adsorbent reactivation device after, return before the flue gas absorber, also introduce the regenerative agent heat exchanger, enter air and the Restore All gas of burner in this preheating.
5. according to the method for claim 1, it is characterized in that all or part of the returning in the flue gas absorber of the regenerative agent of being drawn by the adsorbent reactivation device recycles after cooling.
6. according to the method for claim 1, it is characterized in that the combined feed flow rate of the reducing gas of described introducing adsorbent reactivation device is determined with reference to the concentration of raw material sulphur oxide, nitrogen oxide, be 3～12 times of theoretical consumptions.
7. according to the method for claim 1, it is characterized in that the cooling of high temperature regeneration tail gas and separate out elemental sulfur.
8. according to any method in the claim 1,2,3,5,6 and 7, it is characterized in that described adsorbent is catalytic cracking catalyst.
9. according to the method for claim 4, it is characterized in that described adsorbent is catalytic cracking catalyst.
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| CN103301744B (en) * | 2013-06-17 | 2015-01-14 | 青岛科技大学 | Desulfurization device and method for preparing sulfur particles by removing SO2 from flue gas |
| CN103599788B (en) * | 2013-11-01 | 2015-09-30 | 中国石油化工股份有限公司 | A kind of cobalt-base catalyst for CO hydrogenation and its preparation method and application |
| CN104001403B (en) * | 2014-05-06 | 2016-02-17 | 中国科学院过程工程研究所 | The technique of a kind of activated coke/charcoal flue gas desulfurization and denitrification and recovery elemental sulfur and device |
| CN106268722B (en) * | 2015-05-14 | 2019-04-09 | 中国石油天然气股份有限公司 | Regenerated desorbing agent and its application are carried out to houghite adsorbent |
| CN107970735A (en) * | 2016-10-21 | 2018-05-01 | 中国石油化工股份有限公司 | The processing method and desulfuration adsorbent regeneration method for the tail gas that regenerative sulfur binding adsorbent produces |
| CN108014761B (en) * | 2016-10-31 | 2021-05-14 | 中国石油化工股份有限公司 | Regeneration method of adsorbent and flue gas purification method |
| CN114130154B (en) * | 2020-09-03 | 2023-05-05 | 中国石油化工股份有限公司 | Low-temperature flue gas denitration method and device and flue gas desulfurization and denitration method and device |
| CN114432876B (en) * | 2020-11-05 | 2023-10-31 | 中国石油天然气股份有限公司 | Sulfur dioxide catalytic adsorption regeneration system and method |
| CN113600246A (en) * | 2021-08-23 | 2021-11-05 | 中冶赛迪上海工程技术有限公司 | Desulfurization catalyst regeneration method and system |
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| CN101209391A (en) * | 2006-12-30 | 2008-07-02 | 中国石油化工股份有限公司 | Method for removing oxysulfide and/or nitrogen oxide from flue gas and hydrocarbon oil cracking method |
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