CN104437674B - Regenerating method of catalytic conversion catalyst - Google Patents
Regenerating method of catalytic conversion catalyst Download PDFInfo
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- CN104437674B CN104437674B CN201410694183.1A CN201410694183A CN104437674B CN 104437674 B CN104437674 B CN 104437674B CN 201410694183 A CN201410694183 A CN 201410694183A CN 104437674 B CN104437674 B CN 104437674B
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Abstract
The invention discloses a regenerating method of a catalytic conversion catalyst. The regenerating method comprises the following steps: a catalyst which is transferred from a reactor firstly enters a first generator to be blown and regenerated by first regenerated gas; and a primary regenerant at the outlet of the first generator is conveyed to a catalyst flow distributor and is divided into two material flows which respectively enters a second regenerator and the reactor, wherein the flow of the primary regenerant flow entering the reactor accounts for 1-100% of the total flow of the primary regenerant in the flow and a part of primary regenerant enters a second regenerator to be secondarily regenerated by virtue of second regenerated gas to obtain a secondary regenerant which is combined with the primary regenerant flow and enters the reactor together. According to the regeneration method disclosed by the invention, the capacity of the existing reactor can be effectively improved, frequent charking regeneration of the catalyst is avoided and the regenerating temperature and temperature rise are reduced, and the total service life of the catalyst is prolonged. Moreover, the flow rate of the catalyst in different mobile bed reactors is independently regulated, and the regenerating method can be used in industrial production of methanol to propylene.
Description
Technical field
The present invention relates to a kind of renovation process of catalytic converting catalyst, it is particularly well-suited to the catalysis of moving bed preparing propylene from methanol
The regeneration of agent.
Background technology
During numerous hydrocarbons catalytic conversions, the main reaction occurring have methylation reaction, dehydrogenation, dehydrocyclization,
Isomerization, cracking reaction and carbon deposit reaction etc., wherein carbon deposit reaction can lead to catalyst that invertibity inactivation, this invertibity occur
Inactivation mostlys come from the Carbon spices producing in course of reaction and covers the activated centre of catalyst or plug catalyst
Inside/outside duct.
The formation mechenism of Carbon spices is sufficiently complex, for its formation mechenism of different catalyst different it is however generally that can
To be considered to occur the high-carbon product generating after oligomeric or aromatisation to enter at the activated centre of catalyst due to hydro carbons species
One step dehydrogenation carbonization and formed.The reaction conditions such as reaction temperature, carbon deposit precursor concentration, feed space velocity, power lifetime
There is direct impact on the species of carbon deposit material, content and distribution.
For the preparing propylene from methanol process on zsm-5 molecular sieve catalyst, reaction temperature, these conditions of methyl alcohol air speed are more severe
Carve, catalyst carbon deposit deactivation rate is faster, under the same reaction time, the C/Hratio (c/h) of Carbon spices is with degree of graphitization on the contrary
Lower, in other words, its combustibility of carbon deposit producing under higher reaction severity is more active, can be in relatively low regeneration temperature
Lower by carbon deposit burn off.Meanwhile, there is unstability carbon deposit, reacted carbon deposited catalyst is in the bar of inert gas purge more
Under part, its carbon deposit content can decline, and the Carbon spices coming from molecular weight the reason decline depart from catalyst, and this part is divided
Amount its c/h of less carbon deposit is relatively low for son, and hydrogen content is high, can discharge substantial amounts of heat, removed by inert gas in combustion process
Afterwards decaying catalyst can recovered part activity, activation recovering how relevant with reaction condition at least.
Activity in order to recover deactivation catalyst of carbon deposit is generally passed through to aoxidize the carbon deposit of deposition on burn off catalyst, this mistake
Journey is carried out under the high temperature conditions, and the humidity of regeneration gas, the regeneration temperature and catalyst time of staying in high-temperature region can
Directly affect the speed of its surface area decline, the decline of catalyst surface area is the principal element of impact catalyst life.Carbon deposit
Steam not only can be generated in combustion, and the moment ignition temperature in carbon deposit site can be significantly larger than regeneration gas main body temperature
Degree, this harsh regenerative environ-ment has a significant impact to the stability of catalyst.Therefore, how to reduce catalyst in regenerative process
Loss of activity, improve the regeneration times of catalyst and entire life, become the emphasis of Burning Coke on Catalyst regenerative process research, height
Effect renovation process can not only reducing energy consumption moreover it is possible to increase benefit.
In order to relax regeneration condition, reduce temperature rise of making charcoal, United States Patent (USP) usp 5037785 advises, under oxygen-containing gas, adopting
The method irradiated with laser devokes to catalyst.United States Patent (USP) usp 4202865 suggestion batch (-type) notes oxygen.United States Patent (USP) usp
The area that makes charcoal of regenerator is then set to pyramidal structure by 4859643 and usp 5277880, different axial positions, and bed has
Different thickness, to improve the gas distribution along bed axial location.Top bed is relatively thin, and the tolerance of distribution is larger, lower bed
Layer is thicker, and the tolerance of distribution is less, preferably meets the needs to oxygen for the axially different position, catalyst is on bed top simultaneously
The time of staying of high-temperature region reduces.
Chinese patent cn 102218354 a proposes to be divided into from top to bottom burning soon by the scorch region of moving bed regenerator
Section, changeover portion and superheat section, to solve the shortcomings of in prior art, hydrocarbon conversion catalyst scorch region has temperature runaway risk.China is specially
Sharp cn 1179118 a proposes first by spent agent burn off part carbon deposit in fluid bed at elevated temperatures, then again by part
The catalyst of regeneration is placed in and passes through a furnace area in mobile band, burns down carbon deposit in this region, ensures the short time with this
Control heating to carry out reservation table area, carbon deposit can be completely removed by the heating of long period again.Chinese patent cn
102869447 a propose for the burning of the regeneration catalyzing equipment being used for continuous catalyst regenerating to be distinguished at least two combustion stage,
Each level is divided into n substantially equivalent radial segment, and catalyst passes through to decline dipleg from the first combustion stage under gravity
Section flow direction be vertically located at the section of the second combustion stage below, and the flow process of burning gases make burning gases with
Any order continuously flows through all sections of the first combustion stage, then continuously flows through the institute of the second combustion stage with any order
There is section.
In addition to directly carry out burning carbon removal with oxygen-containing gas, United States Patent (USP) us 5916834 is to for ethylene epoxidizing
The titaniferous multiphase decaying catalyst of reaction is processed using materials such as water, alcohol esters, during eliminating epoxidation of ethylene
The inactivation that the oligomer blocking catalyst duct that ethylene oligomerization generates is caused, has reached the purpose recovering catalyst activity.China
Patent cn1768957 a suggestion was pre-processed with a kind of carbon deposit cleaner before catalyst carries out coke-burning regeneration, to reduce
Carbon deposit content on decaying catalyst, reduces highly exothermic in regenerative process.But the method introduces in spent agent in a large number
Organic washing agent, the removing of cleaning agent is also required to consume extra energy with regeneration.
Regenerative section is in addition to playing the effect of burn off carbon deposit additionally it is possible to enter pre- before reactor as catalyst
Processing meanss, Chinese patent cn 101811071 b passes through to enter auxiliary combustion chamber using oxygen-containing regenerating medium, with combustion medium
Catalytic combustion, the mixed gas that burning generates and remaining regenerating medium carry heat and enter fluid bed regenerator, with inactivation
Catalyst contact carries out coke-burning regeneration it is achieved that the pre- carbon deposit of catalyst, in order to improve low-carbon alkene during preparing propylene from methanol
Yield.
In existing coking deactivation renovation process, most of patents focus on to consider the flow process by changing regenerator and structure
To reduce regeneration severity, so can improve the complexity of regenerative section technique and equipment.Small part patent then proposes to treat
Raw agent carries out washing burnt pretreatment with the carbon content on the catalyst of the device that is lowered into making charcoal, but this kind of method can be in carbon deposited catalyst
The new organic species of upper introducing, increased the complexity of whole technique, once carbon deposit cleaner has not removed on spent agent
Entirely, it will become the new thermal source in regenerator.For some as special hydrocarbon catalyzed conversions in preparing propylene from methanol, methanol-to-olefins etc.
For technique, the catalyst entering reactor needs certain pre- carbon deposit to can be only achieved more preferable selectivity, but for one
In technique, how catalyst, for the technique of movement of connecting between two kinds of different reactors, realizes catalyst stream between two kinds of reactors
While amount difference, reduce Burning Coke on Catalyst regeneration frequency and with severity and improve it selectively, then have no report.
Content of the invention
The purpose of the present invention is for catalyst regeneration frequency present in existing catalytic converting catalyst regeneration techniques
Height, in reaction-regeneration cycle the problems such as rate of catalyst flow modulation poor performance, provides a kind of regeneration side of catalytic converting catalyst
Method.
The renovation process of catalytic converting catalyst is: from reactor, the catalyst f of removal initially enters the first regenerator
In at 170-650 DEG C by the first regeneration gas i carry out purging regeneration, time of staying τ in the first regenerator for the catalyst2
For catalyst reactor time of staying τ10.1-10 times.The one-level regenerative agent a of the first regenerator outlet is delivered to catalyst
It is divided into b, c two streams to respectively enter Second reactivator and reactor after flow distributor, enter the one-level regenerative agent of reactor
The flow of stream stock c accounts for the 1-100% of one-level regenerative agent total flow in stream stock a, and the one-level regenerative agent in stream stock b enters the second regeneration
After in device, the secondary regenerator agent d by obtaining after the second regeneration gas k carries out secondary recycling is merged with one-level regenerative agent stream stock c together
Enter reactor.
The form of described reactor, the first regenerator and Second reactivator is moving-burden bed reactor or fluidized-bed reaction
Device, in the first regenerator the contact form of the first regeneration gas i and reclaimable catalyst be following current, countercurrently, cross-flow or complete mixing flow.Institute
The first regeneration gas i stated is derived from nitrogen, vapor or both mixtures.Described regenerates for first in the first regenerator
Gas crosses 0.1-10 times that a gas speed crosses a gas speed for gas in reactor.Described catalytic converting catalyst active ingredient is molecule
Sieve, metal or both mixtures.In described stream stock c, one-level regeneration agent flux is one-level regeneration agent flux in stream stock a
When 100%, catalyst is 1-5 time through the cycle-index of reactor.Second regeneration gas k of described entrance Second reactivator is
One or more of air, nitrogen, oxygen, vapor.The described reaction raw materials g entering in reactor is hydro carbons or contains
Oxygen compound.The secondary regenerator agent d of described Second reactivator outlet before mixing with one-level regenerative agent c can without or
Person is through one or more moving beds or fluidized-bed reactor.
The present invention compared with prior art has the advantages that
1) Catalytic conversion catalyst regeneration method of the present invention, compared to existing carbon deposited catalyst continuous regeneration method
Speech, its key problem in technology is the pretreatment to carbon deposited catalyst, is purged the low molecular weight part in carbon deposit by inert gas
Remove, it is thus also avoided that original carbon deposited catalyst is directly sent to coke-burning regeneration equipment while recovering catalyst member activity
Coke-burning regeneration, because the low molecule carbon deposit c/h that this part is removed by purging is higher, the combustion heat is big, is to lead to coke-burning regeneration equipment
The key factor of middle overtemperature, the method can avoid the damage of the surface area that catalyst leads in coke-burning regeneration equipment because of overtemperature
Lose；
2) Catalytic conversion catalyst regeneration method of the present invention, carries out regenerating it to carbon deposited catalyst by the first regenerator
Afterwards some or all of one-level regenerative agent is recycled directly back to reactor, greatly reduces the coke-burning regeneration frequency of catalyst, keep away
Exempt from the activated centre irreversible loss that catalyst leads to because of the high temperature in coke combustion, high humidity environment；
3) Catalytic conversion catalyst regeneration method of the present invention, carries out regenerating it to carbon deposited catalyst by the first regenerator
Afterwards some or all of one-level regenerative agent is recycled directly back to reactor, is capable of in a continuous catalyst reaction-again
The coexisting of two kinds of different rate of catalyst flow in raw system, the method is for the technique stream that there are multiple differential responses series connection
Cheng Eryan, is capable of the independent regulation and control of each reaction workshop section catalyst residence times, especially for moving bed methyl alcohol system third
For alkene technique, same catalyst is used in the different reactor of two series connection, and the catalyst stream needed for two reactors
Speed is different；
4) Catalytic conversion catalyst regeneration method of the present invention, carries out regenerating it to carbon deposited catalyst by the first regenerator
Afterwards some or all of one-level regenerative agent is recycled directly back to reactor, because one-level regenerative agent is part carbon deposit agent, for first
Additionally it is possible to play the work improving catalyst performance for this kind of pre- carbon deposit of alcohol propylene can improve the reaction of catalyst choice
With, it is to avoid separately set pre- carbon deposit unit in coke-burning regeneration workshop section, simplify coke-burning regeneration equipment；
5) Catalytic conversion catalyst regeneration method of the present invention, realizes the part of catalyst by the purging of inert gas
Regeneration, for processing the method for decaying catalyst compared to the existing cleaning agent using containing organic matter, it is to avoid cleaning agent
Remove operation again, reduce complexity and the energy consumption of whole technique；
6) Catalytic conversion catalyst regeneration method of the present invention, has very strong adaptation for improving reaction workshop section severity
Property.For preparing propylene from methanol process, improve the feed space velocity of reaction workshop section or reaction temperature can improve propene yield,
But also result in the increase of catalyst carbon deposit speed, catalyst regeneration frequency also increases therewith.Contain in carbon deposit under the conditions of this kind of
There is soft Jiao of low c/h of a large amount of low-molecular-weights, directly that the carbon deposit burn off heat release containing this Some Species is fast, temperature rise is big, to catalysis
The destruction of agent entire life is strong, ensure that the catalyst total longevity under high severity reaction condition by regeneration methods of the invention
Life.
Brief description
Fig. 1 is the renovation process schematic flow sheet of catalytic converting catalyst；
Fig. 2 is Catalytic conversion catalyst regeneration method schematic flow sheet in embodiment 3,4；
In figure, reactor 1, the first regenerator 2, Second reactivator 3, distributor 4, reactor 5, one-level regenerative agent stream stock a,
B, c, secondary regenerator agent stream stock d, one-level regenerative agent and secondary regenerator agent mixed flow stock e, reaction stream stock g, product stream stock h, the
One regeneration gas i, the first regeneration product gas j, the second regeneration gas k, the second regeneration product gas l.
Specific embodiment
The renovation process of catalytic converting catalyst is: from reactor 1, the catalyst f of removal initially enters the first regenerator
At 170-650 DEG C, purging regeneration, the time of staying in the first regenerator 2 for the catalyst are carried out by the first regeneration gas i in 2
τ2For catalyst residence times τ in reactor 110.1-10 times.The one-level regenerative agent a of the first regenerator 2 outlet is delivered to catalysis
It is divided into b, c two streams to respectively enter Second reactivator 3 and reactor 1 after agent flux distributor 4, enter the one-level of reactor 1
The flow of regenerative agent stream stock c accounts for the 1-100% of one-level regenerative agent total flow in stream stock a, and the one-level regenerative agent in stream stock b enters the
The secondary regenerator agent d obtaining after the second regeneration gas k carries out secondary recycling in two regenerators 3 and one-level regenerative agent stream stock c closes
And after together enter reactor 1.
The form of described reactor 1, the first regenerator 2 and Second reactivator 3 is moving-burden bed reactor or fluid bed
Reactor, in the first regenerator 2 contact form of the first regeneration gas i and reclaimable catalyst be following current, countercurrently, cross-flow or entirely mix
Stream.The first described regeneration gas i is derived from nitrogen, vapor or both mixtures.Described in the first regenerator 2
One regeneration gas crosses 0.1-10 times that a gas speed crosses a gas speed for gas in reactor 1.Described catalytic converting catalyst effectively becomes
It is divided into molecular sieve, metal or both mixtures.In described stream stock c, one-level regeneration agent flux is one-level regenerative agent in stream stock a
Flow 100% when, catalyst through reactor 1 cycle-index be 1-5 time.The second of described entrance Second reactivator 3 is again
Angry k is one or more of air, nitrogen, oxygen, vapor.The described reaction raw materials g entering in reactor 1 is hydrocarbon
Class or oxygenatedchemicals.The secondary regenerator agent d of described Second reactivator 3 outlet can before mixing with one-level regenerative agent c
With without or through one or more moving beds or fluidized-bed reactor.
Catalytic conversion catalyst regeneration method of the present invention is described in further detail with specific embodiment in conjunction with accompanying drawing.
Accompanying drawing and specific embodiment do not limit the scope of protection of present invention.
Embodiment 1
From reactor 1, the catalyst f of removal initially enters and passes through the first regeneration gas in the first regenerator 2 at 170 DEG C
I carries out purging regeneration, time of staying τ in the first regenerator 2 for the catalyst2For catalyst residence times τ in reactor 1110
Times.The one-level regenerative agent a of the first regenerator 2 outlet is divided into b, c two streams to enter respectively after being delivered to catalyst flow distributor 4
Enter Second reactivator 3 and reactor 1, the flow entering the one-level regenerative agent stream stock c of reactor 1 accounts for one-level regenerative agent in stream stock a
The 1% of total flow, in the one-level regenerative agent entrance Second reactivator 3 in stream stock b after the second regeneration gas k carries out secondary recycling
The secondary regenerator agent d obtaining together enters reactor 1 after merging with one-level regenerative agent stream stock c.
The form of reactor 1, the first regenerator 2 and Second reactivator 3 is moving-burden bed reactor, the in the first regenerator 2
One regeneration gas i is adverse current with the contact form of reclaimable catalyst.
First regeneration gas i is derived from nitrogen.
Cross 0.1 times that a gas speed crosses a gas speed for gas in reactor 1 for the second regeneration gas in the first regenerator 2.
Catalytic converting catalyst active ingredient is pt/sn supported catalyst.
The second regeneration gas k entering Second reactivator 3 is the mixture of air and nitrogen.
Entering the reaction raw materials g in reactor 1 is hydro carbons.
Embodiment 2
From reactor 1, the catalyst f of removal initially enters and passes through the first regeneration gas in the first regenerator 2 at 650 DEG C
I carries out purging regeneration, time of staying τ in the first regenerator 2 for the catalyst2For catalyst residence times τ in reactor 115
Times.The one-level regenerative agent a of the first regenerator 2 outlet is divided into b, c two streams to enter respectively after being delivered to catalyst flow distributor 4
Enter Second reactivator 3 and reactor 1, the flow entering the one-level regenerative agent stream stock c of reactor 1 accounts for one-level regenerative agent in stream stock a
The 60% of total flow, in the one-level regenerative agent entrance Second reactivator 3 in stream stock b after the second regeneration gas k carries out secondary recycling
The secondary regenerator agent d obtaining together enters reactor 1 after merging with one-level regenerative agent stream stock c.
The form of reactor 1, the first regenerator 2 and Second reactivator 3 is fluidized-bed reactor, the in the first regenerator 2
One regeneration gas i is complete mixing flow with the contact form of reclaimable catalyst.
First regeneration gas i is derived from nitrogen.
Cross 5 times that a gas speed crosses a gas speed for gas in reactor 1 for the first regeneration gas in the first regenerator 2.
Catalytic converting catalyst active ingredient is y type molecular sieve.
The second regeneration gas k entering Second reactivator 3 is the mixture of nitrogen and oxygen.
Entering the reaction raw materials g in reactor 1 is hydro carbons.
Embodiment 3
From reactor 1, the catalyst f of removal initially enters and passes through the first regeneration gas in the first regenerator 2 at 300 DEG C
I carries out purging regeneration, time of staying τ in the first regenerator 2 for the catalyst2For catalyst residence times τ in reactor 11's
0.1 times.The one-level regenerative agent a of the first regenerator 2 outlet is divided into b, c two streams to divide after being delivered to catalyst flow distributor 4
Not Jin Ru Second reactivator 3 and reactor 1, enter reactor 1 one-level regenerative agent stream stock c flow account for stream stock a in one-level again
The 100% of raw agent total flow, is carried out secondary by the second regeneration gas k in the one-level regenerative agent entrance Second reactivator 3 in stream stock b
The secondary regenerator agent d obtaining after regeneration together enters reactor 1 after merging with one-level regenerative agent stream stock c.
The form of reactor 1, the first regenerator 2 and Second reactivator 3 is moving-burden bed reactor, the in the first regenerator 2
One regeneration gas i is cross-flow with the contact form of reclaimable catalyst.
First regeneration gas i is derived from the mixture of nitrogen and vapor.
Cross 5 times that a gas speed crosses a gas speed for gas in reactor 1 for the first regeneration gas in the first regenerator 2.
Catalytic converting catalyst active ingredient is zsm-5 molecular sieve.
Stream stock c in one-level regenerative agent through reactor 1 cycle-index be 1 time.
The second regeneration gas k entering Second reactivator 3 is the mixture of nitrogen and oxygen.
Entering the reaction raw materials g in reactor 1 is oxygenatedchemicals methyl alcohol.
The secondary regenerator agent d of Second reactivator 3 outlet is before mixing with one-level regenerative agent c through a moving bed reaction
Device 5.
Embodiment 4
From reactor 1, the catalyst f of removal initially enters and passes through the first regeneration gas in the first regenerator 2 at 650 DEG C
I carries out purging regeneration, time of staying τ in the first regenerator 2 for the catalyst2For catalyst residence times τ in reactor 11's
0.1 times.The one-level regenerative agent a of the first regenerator 2 outlet is divided into b, c two streams to divide after being delivered to catalyst flow distributor 4
Not Jin Ru Second reactivator 3 and reactor 1, enter reactor 1 one-level regenerative agent stream stock c flow account for stream stock a in one-level again
The 100% of raw agent total flow, is carried out secondary by the second regeneration gas k in the one-level regenerative agent entrance Second reactivator 3 in stream stock b
The secondary regenerator agent d obtaining after regeneration together enters reactor 1 after merging with one-level regenerative agent stream stock c.
The form of reactor 1, the first regenerator 2 and Second reactivator 3 is fluidized reactor, first in the first regenerator 2
Regeneration gas i is complete mixing flow with the contact form of reclaimable catalyst.
First regeneration gas i is derived from nitrogen.
Cross 10 times that a gas speed crosses a gas speed for gas in reactor 1 for the first regeneration gas in the first regenerator 2.
Catalytic converting catalyst active ingredient is zsm-5 molecular sieve.
Stream stock c in one-level regenerate agent flux through reactor 1 cycle-index be 5 times.
The second regeneration gas k entering Second reactivator 3 is the mixture of air and nitrogen.
Enter the mixture that the reaction raw materials g in reactor 1 is oxygenatedchemicals methyl alcohol and dimethyl ether.
The secondary regenerator agent d of Second reactivator 3 outlet is before mixing with one-level regenerative agent c through a fluidized-bed reaction
Device 5.
Claims (6)
1. a kind of renovation process of catalytic converting catalyst it is characterised in that: from reactor (1), the catalyst (f) of removal is first
It is introduced in the first regenerator (2) and to pass through the first regeneration gas at 170-650 DEG C and (i) carry out purging regeneration, catalyst is first
Time of staying τ in regenerator (2)2For catalyst residence times τ in reactor (1)10.1-10 times, the first regenerator (2) goes out
One-level regenerative agent stream stock (a) of mouth is divided into first-class stock (b), second stock (c) two after being delivered to catalyst flow distributor (4)
Second reactivator (3) and reactor (1) is respectively enterd, the flow entering second stock (c) of reactor (1) accounts for one after stock logistics
In level regenerative agent stream stock (a), the ratio of one-level regenerative agent total flow is more than or equal to 1% and is less than 100%, in first-class stock (b)
Level regenerative agent enters secondary regenerator agent (d) obtaining after the second regeneration gas (k) carries out secondary recycling in Second reactivator (3)
Enter in reactor (5), after merging with second stock (c), together enter reactor (1)；The first described regeneration gas is (i) derived from
Nitrogen, vapor or both mixtures.
2. as claimed in claim 1 a kind of renovation process of catalytic converting catalyst it is characterised in that described reactor
(1), the form of the first regenerator (2) and Second reactivator (3) is moving-burden bed reactor or fluidized-bed reactor, the first regeneration
In device (2) the first regeneration gas (i) with the contact form of reclaimable catalyst be following current, countercurrently, cross-flow or complete mixing flow.
3. as claimed in claim 1 a kind of renovation process of catalytic converting catalyst it is characterised in that described for first
The first regeneration gas in regenerator (2) crosses 0.1-10 times that a gas speed crosses a gas speed for gas in reactor (1).
4. as claimed in claim 1 a kind of renovation process of catalytic converting catalyst it is characterised in that described catalyzed conversion
Catalyst active ingredient is molecular sieve, metal or both mixtures.
5. as claimed in claim 1 a kind of renovation process of catalytic converting catalyst it is characterised in that described entrance second
Second regeneration gas (k) of regenerator (3) is one or more of air, nitrogen, oxygen, vapor.
6. as claimed in claim 1 a kind of renovation process of catalytic converting catalyst it is characterised in that enter reactor (1)
In reaction raw materials (g) be hydro carbons or oxygenatedchemicals.
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| US4859643A (en) * | 1988-05-11 | 1989-08-22 | Uop | Regeneration method with reduced catalyst heat exposure |
| CN101391234B (en) * | 2008-10-30 | 2011-05-25 | 石宝珍 | Catalyst multistage regeneration method and device |
| CN103028450B (en) * | 2011-09-30 | 2016-03-02 | 中国石油化工股份有限公司 | catalytic conversion catalyst regeneration method |
| CN103446959B (en) * | 2012-06-04 | 2015-07-29 | 中国石油化工股份有限公司 | A kind of fluidized-bed reactor with charging heat exchange, reaction regeneration device and application thereof |
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