CN104437674A - Regenerating method of catalytic conversion catalyst - Google Patents
Regenerating method of catalytic conversion catalyst Download PDFInfo
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- CN104437674A CN104437674A CN201410694183.1A CN201410694183A CN104437674A CN 104437674 A CN104437674 A CN 104437674A CN 201410694183 A CN201410694183 A CN 201410694183A CN 104437674 A CN104437674 A CN 104437674A
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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, be specially adapted to the regeneration of moving bed catalyst for producing propylene with methanol.
Background technology
In numerous hydrocarbons catalytic conversion processes, the reaction of main generation has methylation reaction, dehydrogenation, dehydrocyclization, isomerization, cracking reaction and carbon deposit reaction etc., wherein carbon deposit reaction can cause catalyst generation invertibity inactivation, and this invertibity inactivation mainly comes from the Carbon spices produced in course of reaction and covers the activated centre of catalyst or plug the inside/outside duct of catalyst.
The formation mechenism of Carbon spices is very complicated, different for its formation mechenism of different catalyst, generally speaking can think that the further dehydrogenation carbonization of high-carbon product generated after oligomeric or aromatisation occur at the activated centre place of catalyst due to hydro carbons species is formed.The reaction condition such as reaction temperature, carbon deposit precursor concentration, feed space velocity, power lifetime has direct impact to the kind of carbon deposit material, concentration 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 harsher, catalyst carbon deposit deactivation rate is faster, under the same reaction time, the C/Hratio (C/H) of Carbon spices is lower on the contrary with degree of graphitization, in other words, its combustibility of carbon deposit produced under higher reaction severity is more active, can by carbon deposit burn off under lower regeneration temperature.Meanwhile, carbon deposit has unstability more, reacted carbon deposited catalyst its carbon deposit content under the condition of inert gas purge can decline, the Carbon spices that the reason declined comes from molecular weight departs from catalyst, its C/H is lower for the carbon deposit of this part molecular weight, and hydrogen content is high, can discharge a large amount of heat in combustion process, after being removed by inert gas decaying catalyst can recovered part active, activation recovering number then relevant with reaction condition.
In order to recover the carbon deposit of activity usually by oxidation burn off catalyst deposits of deactivation catalyst of carbon deposit, this process is carried out under the high temperature conditions, the humidity of regeneration gas, regeneration temperature and catalyst directly can affect in the time of staying of high-temperature region the speed that its surface area declines, and the decline of catalyst surface area is the principal element affecting catalyst life.Carbon deposit not only can generate steam in combustion, and carbon deposit site moment ignition temperature can far away higher than regeneration gas body temperature, the stability of regenerative environ-ment to catalyst of this harshness has a significant impact.Therefore, how to reduce the loss of activity of catalyst in regenerative process, improve regeneration times and the entire life of catalyst, become the emphasis of Burning Coke on Catalyst regenerative process research, efficient renovation process can not only reduce energy consumption, can also improve effects.
In order to relax regeneration condition, reduce temperature rise of making charcoal, US Patent No. P 5037785 advises under oxygen-containing gas, adopts and swashs light-struck method to catalyst decoking.US Patent No. P 4202865 suggestion batch (-type) notes oxygen.The district that makes charcoal of regenerator is set to pyramidal structure, different axial positions by US Patent No. P 4859643 and USP 5277880, and bed has different thickness, to improve the distribution of gas along bed axial location.Top bed is thinner, and the tolerance of distribution is comparatively large, and bottom bed is thicker, and the tolerance of distribution is less, meets the needs of axially different position to oxygen preferably, and catalyst reduced in the time of staying in bed upper pyrometer district simultaneously.
Chinese patent CN 102218354 A proposes the scorch region of moving bed regenerator to be divided into the section of burning, changeover portion and superheat section soon from top to bottom successively, there is the shortcomings such as temperature runaway risk to solve hydrocarbon conversion catalyst scorch region in prior art.Chinese patent CN 1179118 A proposes first by spent agent burn off part carbon deposit in fluid bed at elevated temperatures, and then the catalyst of partial regeneration is placed on moving belt by a furnace area, in this region, carbon deposit is burnt down, ensure that the control heating of short time carrys out reservation table area with this, the heating again by the long period comes completely except carbon deposition removal.Chinese patent CN 102869447 A proposes the combustion zone of the regeneration catalyzing equipment being used for continuous catalyst regenerating to be divided at least two combustion stage, each grade is divided into N number of substantially equivalent radial segment, catalyst flows to the section of the second combustion stage be vertically positioned at below it under gravity from the section of the first combustion stage by decline dipleg, and the flow process of burning gases makes burning gases continuously flow through all sections of the first combustion stage with any order, then continuously flows through all sections of the second combustion stage with any order.
Except direct oxygen-containing gas carries out burning carbon removal, US Patent No. 5916834 adopts the material such as water, alcohol ester to process to the heterogeneous decaying catalyst of titaniferous for epoxidation of ethylene, with the inactivation that the oligomer blocking catalyst duct of eliminating ethylene oligomerization generation in epoxidation of ethylene process is caused, reach the object recovering catalyst activity.Chinese patent CN1768957 A suggestion carried out pretreatment with a kind of carbon deposit cleaner before catalyst carries out coke-burning regeneration, to reduce the carbon deposit content on decaying catalyst, reduced a large amount of heat releases in regenerative process.But the method introduces a large amount of organic washing agent in spent agent, removing of cleaning agent also needs to consume extra energy with regenerating.
Regenerative section is except playing the effect of burn off carbon deposit, pretreatment unit before can also entering reactor as catalyst, Chinese patent CN 101811071 B enters auxiliary combustion chamber by adopting containing oxygen regenerating medium, with combustion medium catalytic combustion, the mist that burning generates and remaining regenerating medium carry heat and enter fluid bed regenerator, contact with decaying catalyst and carry out coke-burning regeneration, achieve the pre-carbon deposit of catalyst, in order to improve yield of light olefins in preparing propylene from methanol process.
In existing coking deactivation renovation process, most of patent considers that emphatically the flow process and structure by changing regenerator reduces regeneration severity, can improve the complexity of regenerative section technique and equipment like this.Small part patent then proposes to wash burnt pretreatment to spent agent and enters the carbon content of making charcoal on the catalyst of device to reduce, but this kind of method can introduce new organic species on carbon deposited catalyst, add the complexity of whole technique, once carbon deposit cleaner does not remove completely on spent agent, the new thermal source in regenerator will be become.For the hydrocarbon catalytic conversion process that some are as special in preparing propylene from methanol, methanol-to-olefins etc., the catalyst entering reactor needs certain pre-carbon deposit just can reach better selective, but for catalyst in a technique connect between two kinds of different reactors movement technique for, how to realize between two kinds of reactors while catalyst flow difference, reduce Burning Coke on Catalyst regeneration frequency and severity and improve that it is selective, then having no report.
Summary of the invention
The catalyst regeneration frequency that the object of the invention is for existing in existing catalytic converting catalyst regeneration techniques is high, and in reaction-regeneration cycle, the problem such as rate of catalyst flow modulation poor performance, provides a kind of renovation process of catalytic converting catalyst.
The renovation process of catalytic converting catalyst is: first the catalyst f shifted out from reactor enters in the first regenerator and at 170-650 DEG C, carry out purging regeneration by the first regeneration gas i, the time of staying τ of catalyst in the first regenerator
2for catalyst reactor time of staying τ
10.1-10 doubly.B, c two bursts of logistics are divided into enter Second reactivator and reactor respectively after the one-level regenerative agent a of the first regenerator outlet is delivered to catalyst flow distributor, the flow entering the one-level regenerative agent stream stock c of reactor accounts for the 1-100% of one-level regenerative agent total flow in stream stock a, together enters reactor after the secondary regenerator agent d that the one-level regenerative agent in stream stock b obtains after entering and carrying out secondary recycling by the second regeneration gas k in Second reactivator and one-level regenerative agent stream stock c merges.
The form of described reactor, the first regenerator and Second reactivator is moving-burden bed reactor or fluidized-bed reactor, and in the first regenerator, the contact form of the first regeneration gas i and reclaimable catalyst is following current, adverse current, cross-flow or complete mixing flow.The first described regeneration gas i is from nitrogen, steam or both mixtures.Described cross a gas speed for gas in reactor for the first regeneration gas in the first regenerator and cross a 0.1-10 of gas speed doubly.Described catalytic converting catalyst active ingredient is molecular sieve, metal or both mixtures.When in described stream stock c, one-level regenerative agent flow is 100% of one-level regenerative agent flow in stream stock a, catalyst through the cycle-index of reactor be 1-5 time.Described the second regeneration gas k entering Second reactivator is one or more in air, nitrogen, oxygen, steam.The described reaction raw materials g entered in reactor is hydro carbons or oxygenatedchemicals.The secondary regenerator agent d of described Second reactivator outlet before mixing with one-level regenerative agent c can without or through one or more moving bed or fluidized-bed reactor.
The beneficial effect that the present invention compared with prior art has:
1) Catalytic conversion catalyst regeneration method of the present invention, compared to existing carbon deposited catalyst continuous regeneration method, its key problem in technology is the pretreatment to carbon deposited catalyst, by inert gas, the low molecular weight part purging in carbon deposit is removed, while recovery catalyst member activity, also avoid and original carbon deposited catalyst is directly sent to coke-burning regeneration equipment coke-burning regeneration, because it is higher that this part is purged the low molecule carbon deposit C/H removed, the combustion heat is large, it is the key factor causing overtemperature in coke-burning regeneration equipment, the loss of the surface area that the method can be avoided catalyst in coke-burning regeneration equipment causing because of overtemperature,
2) Catalytic conversion catalyst regeneration method of the present invention, after by the first regenerator carbon deposited catalyst being regenerated, some or all of one-level regenerative agent direct circulation is returned reactor, greatly reduce the coke-burning regeneration frequency of catalyst, avoid the activated centre irreversible loss that catalyst causes because of the high temperature in coke combustion, high humidity environment;
3) Catalytic conversion catalyst regeneration method of the present invention, after by the first regenerator carbon deposited catalyst being regenerated, some or all of one-level regenerative agent direct circulation is returned reactor, coexisting of two kinds of different rate of catalyst flow can be realized in a continuous print catalyst reaction-regenerative system, the method is for a technological process that there is multiple differential responses series connection, the independent regulation and control of each reaction workshop section catalyst residence times can be realized, particularly for moving bed process for preparing propylene from methanol, same catalyst is used in the different reactor of two series connection, and the rate of catalyst flow difference needed for two reactors,
4) Catalytic conversion catalyst regeneration method of the present invention, after by the first regenerator carbon deposited catalyst being regenerated, some or all of one-level regenerative agent direct circulation is returned reactor, because one-level regenerative agent is the agent of part carbon deposit, can improve for the reaction of catalyst choice for this kind of pre-carbon deposit of preparing propylene from methanol, the effect improving catalyst performance can also be played, avoid separately establishing 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, the partial regeneration of catalyst is realized by the purging of inert gas, compared to the method for existing use containing organic cleaning agent process decaying catalyst, what avoid cleaning agent removes operation again, reduces complexity and the energy consumption of whole technique;
6) Catalytic conversion catalyst regeneration method of the present invention, has very strong adaptability for raising reaction workshop section severity.For preparing propylene from methanol process, the feed space velocity or the reaction temperature that improve reaction workshop section can improve propene yield, but also can cause the increase of catalyst carbon deposit speed, and catalyst regeneration frequency also increases thereupon.Containing soft Jiao of a large amount of low-molecular-weight low C/H in carbon deposit under this kind of condition, directly by fast for the carbon deposit burn off heat release containing this part species, temperature rise is large, strong to the destruction of catalyst entire life, can be ensured the catalyst entire life under high severity reaction condition by regeneration methods of the invention.
Accompanying drawing explanation
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 logistics stock g, product stream stock h, the first regeneration gas i, the first regeneration product gas j, second regeneration gas k, the second regeneration product gas l.
Detailed description of the invention
The renovation process of catalytic converting catalyst is: first the catalyst f shifted out from reactor 1 enters in the first regenerator 2 and at 170-650 DEG C, carry out purging regeneration by the first regeneration gas i, the time of staying τ of catalyst in the first regenerator 2
2for catalyst residence times τ in reactor 1
10.1-10 doubly.B, c two bursts of logistics are divided into enter Second reactivator 3 and reactor 1 respectively after the one-level regenerative agent a that first regenerator 2 exports is delivered to catalyst flow distributor 4, the flow entering the one-level regenerative agent stream stock c of reactor 1 accounts for the 1-100% of one-level regenerative agent total flow in stream stock a, together enters reactor 1 after the secondary regenerator agent d that the one-level regenerative agent in stream stock b obtains after entering and carrying out secondary recycling by the second regeneration gas k in Second reactivator 3 and one-level regenerative agent stream stock c merges.
Described reactor 1, first regenerator 2 and the form of Second reactivator 3 are moving-burden bed reactor or fluidized-bed reactor, and in the first regenerator 2, the contact form of the first regeneration gas i and reclaimable catalyst is following current, adverse current, cross-flow or complete mixing flow.The first described regeneration gas i is from nitrogen, steam or both mixtures.Described cross a gas speed for gas in reactor 1 for the first regeneration gas in the first regenerator 2 and cross a 0.1-10 of gas speed doubly.Described catalytic converting catalyst active ingredient is molecular sieve, metal or both mixtures.When in described stream stock c, one-level regenerative agent flow is 100% of one-level regenerative agent flow in stream stock a, catalyst through the cycle-index of reactor 1 be 1-5 time.Described the second regeneration gas k entering Second reactivator 3 is one or more in air, nitrogen, oxygen, steam.The described reaction raw materials g entered in reactor 1 is hydro carbons or oxygenatedchemicals.The secondary regenerator agent d that described Second reactivator 3 exports before mixing with one-level regenerative agent c can without or through one or more moving bed or fluidized-bed reactor.
With detailed description of the invention, Catalytic conversion catalyst regeneration method of the present invention is described in further detail by reference to the accompanying drawings.Accompanying drawing and detailed description of the invention do not limit the scope of protection of present invention.
Embodiment 1
First the catalyst f shifted out from reactor 1 enters in the first regenerator 2 and at 170 DEG C, carries out purging regeneration by the first regeneration gas i, the time of staying τ of catalyst in the first regenerator 2
2for catalyst residence times τ in reactor 1
110 times.B, c two bursts of logistics are divided into enter Second reactivator 3 and reactor 1 respectively after the one-level regenerative agent a that first regenerator 2 exports is delivered to catalyst flow distributor 4, the flow entering the one-level regenerative agent stream stock c of reactor 1 accounts for 1% of one-level regenerative agent total flow in stream stock a, together enters reactor 1 after the secondary regenerator agent d that the one-level regenerative agent in stream stock b obtains after entering and carrying out secondary recycling by the second regeneration gas k in Second reactivator 3 and one-level regenerative agent stream stock c merges.
The form of reactor 1, first regenerator 2 and Second reactivator 3 is moving-burden bed reactor, and in the first regenerator 2, the contact form of the first regeneration gas i and reclaimable catalyst is adverse current.
First regeneration gas i is from nitrogen.
Crossing a gas speed for the second regeneration gas in the first regenerator 2 is 0.1 times that in reactor 1, gas crosses a gas speed.
Catalytic converting catalyst active ingredient is Pt/Sn supported catalyst.
The the second regeneration gas k entering Second reactivator 3 is the mixture of air and nitrogen.
The reaction raw materials g entered in reactor 1 is hydro carbons.
Embodiment 2
First the catalyst f shifted out from reactor 1 enters in the first regenerator 2 and at 650 DEG C, carries out purging regeneration by the first regeneration gas i, the time of staying τ of catalyst in the first regenerator 2
2for catalyst residence times τ in reactor 1
15 times.B, c two bursts of logistics are divided into enter Second reactivator 3 and reactor 1 respectively after the one-level regenerative agent a that first regenerator 2 exports is delivered to catalyst flow distributor 4, the flow entering the one-level regenerative agent stream stock c of reactor 1 accounts for 60% of one-level regenerative agent total flow in stream stock a, together enters reactor 1 after the secondary regenerator agent d that the one-level regenerative agent in stream stock b obtains after entering and carrying out secondary recycling by the second regeneration gas k in Second reactivator 3 and one-level regenerative agent stream stock c merges.
The form of reactor 1, first regenerator 2 and Second reactivator 3 is fluidized-bed reactor, and in the first regenerator 2, the contact form of the first regeneration gas i and reclaimable catalyst is complete mixing flow.
First regeneration gas i is from nitrogen.
Crossing a gas speed for the first regeneration gas in the first regenerator 2 is 5 times that in reactor 1, gas crosses a gas speed.
Catalytic converting catalyst active ingredient is Y zeolite.
The the second regeneration gas k entering Second reactivator 3 is the mixture of nitrogen and oxygen.
The reaction raw materials g entered in reactor 1 is hydro carbons.
Embodiment 3
First the catalyst f shifted out from reactor 1 enters in the first regenerator 2 and at 300 DEG C, carries out purging regeneration by the first regeneration gas i, the time of staying τ of catalyst in the first regenerator 2
2for catalyst residence times τ in reactor 1
10.1 times.B, c two bursts of logistics are divided into enter Second reactivator 3 and reactor 1 respectively after the one-level regenerative agent a that first regenerator 2 exports is delivered to catalyst flow distributor 4, the flow entering the one-level regenerative agent stream stock c of reactor 1 accounts for 100% of one-level regenerative agent total flow in stream stock a, together enters reactor 1 after the secondary regenerator agent d that the one-level regenerative agent in stream stock b obtains after entering and carrying out secondary recycling by the second regeneration gas k in Second reactivator 3 and one-level regenerative agent stream stock c merges.
The form of reactor 1, first regenerator 2 and Second reactivator 3 is moving-burden bed reactor, and in the first regenerator 2, the contact form of the first regeneration gas i and reclaimable catalyst is cross-flow.
First regeneration gas i is from the mixture of nitrogen and steam.
Crossing a gas speed for the first regeneration gas in the first regenerator 2 is 5 times that in reactor 1, gas crosses a gas speed.
Catalytic converting catalyst active ingredient is ZSM-5 molecular sieve.
In stream stock c, one-level regenerative agent is 1 time through the cycle-index of reactor 1.
The the second regeneration gas k entering Second reactivator 3 is the mixture of nitrogen and oxygen.
The reaction raw materials g entered in reactor 1 is oxygenatedchemicals methyl alcohol.
Second reactivator 3 export secondary regenerator agent d before mixing with one-level regenerative agent c through a moving-burden bed reactor 5.
Embodiment 4
First the catalyst f shifted out from reactor 1 enters in the first regenerator 2 and at 650 DEG C, carries out purging regeneration by the first regeneration gas i, the time of staying τ of catalyst in the first regenerator 2
2for catalyst residence times τ in reactor 1
10.1 times.B, c two bursts of logistics are divided into enter Second reactivator 3 and reactor 1 respectively after the one-level regenerative agent a that first regenerator 2 exports is delivered to catalyst flow distributor 4, the flow entering the one-level regenerative agent stream stock c of reactor 1 accounts for 100% of one-level regenerative agent total flow in stream stock a, together enters reactor 1 after the secondary regenerator agent d that the one-level regenerative agent in stream stock b obtains after entering and carrying out secondary recycling by the second regeneration gas k in Second reactivator 3 and one-level regenerative agent stream stock c merges.
The form of reactor 1, first regenerator 2 and Second reactivator 3 is fluidized reactor, and in the first regenerator 2, the contact form of the first regeneration gas i and reclaimable catalyst is complete mixing flow.
First regeneration gas i is from nitrogen.
Crossing a gas speed for the first regeneration gas in the first regenerator 2 is 10 times that in reactor 1, gas crosses a gas speed.
Catalytic converting catalyst active ingredient is ZSM-5 molecular sieve.
In stream stock c, one-level regenerative agent flow is 5 times through the cycle-index of reactor 1.
The the second regeneration gas k entering Second reactivator 3 is the mixture of air and nitrogen.
The reaction raw materials g entered in reactor 1 is the mixture of oxygenatedchemicals methyl alcohol and dimethyl ether.
Second reactivator 3 export secondary regenerator agent d before mixing with one-level regenerative agent c through a fluidized-bed reactor 5.
Claims (9)
1. the renovation process of a catalytic converting catalyst, it is characterized in that: the catalyst (f) shifted out from reactor (1) first enters in the first regenerator (2) and at 170-650 DEG C, (i) carries out purging regeneration by the first regeneration gas, the time of staying τ of catalyst in the first regenerator (2)
2for catalyst residence times τ in reactor (1)
10.1-10 doubly, one-level regenerative agent (a) that first regenerator (2) exports is divided into (b) after being delivered to catalyst flow distributor (4), c () two bursts of logistics enter Second reactivator (3) and reactor (1) respectively, the flow entering one-level regenerative agent stream stock (c) of reactor (1) accounts for the 1-100% of one-level regenerative agent total flow in stream stock (a), reactor (1) is together entered after secondary regenerator agent (d) that one-level regenerative agent in stream stock (b) obtains after entering and carrying out secondary recycling by the second regeneration gas (k) in Second reactivator (3) merges with one-level regenerative agent stream stock (c).
2. the renovation process of a kind of catalytic converting catalyst as claimed in claim 1, it is characterized in that, the form of described reactor (1), the first regenerator (2) and Second reactivator (3) is moving-burden bed reactor or fluidized-bed reactor, and in the first regenerator (2), the first regeneration gas is (i) following current, adverse current, cross-flow or complete mixing flow with the contact form of reclaimable catalyst.
3. the renovation process of a kind of catalytic converting catalyst as claimed in claim 1, is characterized in that, the first described regeneration gas is (i) from nitrogen, steam or both mixtures.
4. the renovation process of a kind of catalytic converting catalyst as claimed in claim 1, is characterized in that, described cross a gas speed for gas in reactor (1) for the first regeneration gas in the first regenerator (2) and crosses a 0.1-10 of gas speed doubly.
5. the renovation process of a kind of catalytic converting catalyst as claimed in claim 1, is characterized in that, described catalytic converting catalyst active ingredient is molecular sieve, metal or both mixtures.
6. the renovation process of a kind of catalytic converting catalyst as claimed in claim 1, it is characterized in that, when one-level regenerative agent flow be 100% of the middle one-level regenerative agent flow of stream stock (a) in described stream stock (c), catalyst through the cycle-index of reactor (1) be 1-5 time.
7. the renovation process of a kind of catalytic converting catalyst as claimed in claim 1, is characterized in that, described the second regeneration gas (k) entering Second reactivator (3) is air, one or more in nitrogen, oxygen, steam.
8. the renovation process of a kind of catalytic converting catalyst as claimed in claim 1, is characterized in that, the described reaction raw materials (g) entered in reactor (1) is hydro carbons or oxygenatedchemicals.
9. the renovation process of a kind of catalytic converting catalyst as claimed in claim 1, it is characterized in that, secondary regenerator agent (d) that described Second reactivator (3) exports before mixing with one-level regenerative agent (c) can without or through one or more moving bed or fluidized-bed reactor.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104991543A (en) * | 2015-07-23 | 2015-10-21 | 北京石油化工工程有限公司 | Moving bed catalyst continuous regeneration control system BRCS |
| CN109694298A (en) * | 2017-10-20 | 2019-04-30 | 中国石油化工股份有限公司 | The method that methanol converts hydrocarbon processed |
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| CN101391234A (en) * | 2008-10-30 | 2009-03-25 | 石宝珍 | Catalyst multistage regeneration method and device |
| CN103028450A (en) * | 2011-09-30 | 2013-04-10 | 中国石油化工股份有限公司 | Catalytic conversion catalyst regeneration method |
| CN103446959A (en) * | 2012-06-04 | 2013-12-18 | 中国石油化工股份有限公司 | Fluidized bed reactor with feeding heat exchange, reaction regenerating device and applications thereof |
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| EP0413857A1 (en) * | 1988-05-11 | 1991-02-27 | Uop | Catalyst regeneration with reduced thermal damage |
| CN101391234A (en) * | 2008-10-30 | 2009-03-25 | 石宝珍 | Catalyst multistage regeneration method and device |
| CN103028450A (en) * | 2011-09-30 | 2013-04-10 | 中国石油化工股份有限公司 | Catalytic conversion catalyst regeneration method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104991543A (en) * | 2015-07-23 | 2015-10-21 | 北京石油化工工程有限公司 | Moving bed catalyst continuous regeneration control system BRCS |
| CN104991543B (en) * | 2015-07-23 | 2017-10-27 | 北京石油化工工程有限公司 | A kind of movable bed catalyst cyclic regeneration control system BRCS |
| CN109694298A (en) * | 2017-10-20 | 2019-04-30 | 中国石油化工股份有限公司 | The method that methanol converts hydrocarbon processed |
| CN109694298B (en) * | 2017-10-20 | 2021-12-28 | 中国石油化工股份有限公司 | Method for preparing hydrocarbon by converting methanol |
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