CN103228357A - Method of regenerating zeolite catalyst - Google Patents
Method of regenerating zeolite catalyst Download PDFInfo
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- CN103228357A CN103228357A CN2011800572626A CN201180057262A CN103228357A CN 103228357 A CN103228357 A CN 103228357A CN 2011800572626 A CN2011800572626 A CN 2011800572626A CN 201180057262 A CN201180057262 A CN 201180057262A CN 103228357 A CN103228357 A CN 103228357A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
- B01J29/7007—Zeolite Beta
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
- B01J29/7034—MTW-type, e.g. ZSM-12, NU-13, TPZ-12 or Theta-3
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
- B01J29/7046—MTT-type, e.g. ZSM-23, KZ-1, ISI-4 or EU-13
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
- B01J29/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing iron group metals, noble metals or copper
- B01J29/74—Noble metals
- B01J29/7469—MTW-type, e.g. ZSM-12, NU-13, TPZ-12 or Theta-3
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/90—Regeneration or reactivation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
- B01J38/12—Treating with free oxygen-containing gas
- B01J38/14—Treating with free oxygen-containing gas with control of oxygen content in oxidation gas
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
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- Chemical Kinetics & Catalysis (AREA)
- Crystallography & Structural Chemistry (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
According to the invention, there is provided a process for regeneration of a catalyst used for a hydrocarbon conversion process. In embodiments, the process comprises a regeneration procedure comprising a controlled oxygen burn ''in-situ'' to the process reactor.
Description
The cross reference of related application
The application requires the priority of the U.S. Provisional Patent Application submitted on November 30th, 2010 number 61/418,212, and its disclosure all is incorporated herein by reference.
Invention field
The present invention relates to the regeneration of zeolite catalyst.
Background of invention
Many hydroconversion process, for example light olefin is to the more conversion of higher alkene, and oxygenate is to the conversion of gasoline, and methylated aromatic compounds is to the disproportionation and the transalkylation of dimethylbenzene, with the hydration of propylene, advantageously use zeolite catalyst to carry out to isopropyl alcohol and Di Iso Propyl Ether.Such catalyst comprises ZSM-5, β, and ZSM-12, ZSM-23, one or more in modenite and other zeolite, described zeolite can have one or more metals that combine with it, for example so-called noble metal such as platinum.In technical process, these catalyst accumulation coke, for example to about 30wt% or even higher level, cause significant inactivation.Depend on described technology and catalyst, the zeolite catalyst of such inactivation can be reproduced, at least to a certain extent.Typically, described inactivation and regeneration cycle take place, one-period in many years to several months or even the level of a couple of days.
United States Patent (USP) 6,380 has been set forth a kind of such regeneration techniques in 119.
One of problem that runs in described inactivation and regeneration cycle is that if use oxygen/noble gas mixtures to burn coke, significant permanent deactivation may take place because of steam treatment at elevated temperatures.The inventor has been found that a kind of method of the zeolite of regenerating, and this method alleviates hydro-thermal steam inactivation.
Summary of the invention
The present invention relates to the regeneration of zeolite catalyst.
In one embodiment, described renovation process alleviates hydro-thermal steam inactivation.
In one embodiment, described zeolite catalyst comprises one or more metals.
In one embodiment, described hydroconversion process comprises the first hydrocarbon feed stream and the fixed bde catalyst that comprises at least a zeolite contacting under the condition that is enough to transform described first feed stream to the second and different feed stream.
In one embodiment, described feed stream comprises non-aromatic hydrocarbon, aromatic hydrocarbon and contain in the one or more heteroatomic hydrocarbon that is selected from oxygen, sulphur, nitrogen and their mixture one or more.
In one embodiment, described catalyst comprises and is selected from ZSM-5, β, ZSM-12, ZSM-23, the zeolite of one or more in the modenite.
In one embodiment, described catalyst comprises one or more metals, preferably includes at least a noble metal, more preferably at least a in platinum, palladium, rhodium, the ruthenium.In other embodiment preferred, described one or more metals are selected from copper, silver, tin and their mixture, randomly also contain at least a noble metal.
An object of the present invention is by providing improved renovation process to improve and/or prolong catalysqt deactivation and regeneration cycle, one or more metals are incorporated in the described catalyst or under the situation on the described catalyst therein, reduce the agglomeration of described one or more metals, this improves described catalyst at hydrocarbon, particularly one or more indications of the activity in the aromatic hydrocarbon method for transformation.
Another object of the present invention is to allow described life of catalyst (process cycles number) to be lengthened to surpass by using with regard to temperature and more harsh other program (ex situ and other program) obtainable life-span of water partial pressure.
With reference to following detailed description, embodiment preferred, embodiment and appended claims, these and other objects, feature and advantage will become apparent.
Describe in detail
According to the present invention, provide regeneration to be used for the method for the catalyst of hydroconversion process.
In some embodiments, described method comprises the reproducer of " original position " oxygen calcination that comprises described process reactor inner control.The strictness control of described " original position " aspect allowable temperature, water partial pressure and oxygen content.Be appreciated that the detail of described program by following detailed explanation of reference and specific embodiment.Grasp and of the present disclosurely it will be understood by those skilled in the art that described method can put into practice to be different from herein the following concrete mode of setting forth.
(1) when described system not when hydrocarbonaceous and water, original position causes the oxygen calcination of described catalyst.The temperature of reactor should be low, and about 650-700/340-370 ° C adopts oxygen content in the gas of 0.5 volume % (all the other are nitrogen) in the porch of reactor beds.In some embodiments, the effluent separator should move under alap temperature, and is consistent with the temperature of described entire system, and the water of accumulation is regularly got rid of.In preferred embodiments, recyclegas also can pass through mole sieve drier, but this is optional.Described regeneration is carried out under 50-200psig.Temperature rise should not surpass 100/55 ° C (less temperature rise is better), and is controlled by regulating described reactor inlet oxygen content.Dry air is incorporated in the reactor feed gas, to regulate the inlet oxygen content.Described regeneration is carried out, and does not simultaneously have oxygen or the inlet oxygen content of certain mark is arranged in exit gas at reactor exit.Described inlet regeneration gas charging rate is about 0.5 to 2.0NM
3/ hr/kg catalyst.
(2) when exit gas reaches the inlet gas oxygen concentration of 70-80%, the inlet temperature of described bed is brought up to about 750/400 ° C.The oxygen content that will enter the mouth remains on 0.5% volume.The main body of coke calcination should take place in step (1) and (2).
(3) when exit gas reaches the inlet gas oxygen concentration of 70-80% once more, the oxygen concentration that will enter the mouth is increased to 1.0 volume %, and with inlet temperature remain on 750/400 ° C (yet, if lower temperature support is burnt basically, promptly about 50% or more oxygen expenditure, described inlet temperature can be lowered).Do not allow any bed tempertaure to surpass 850/450 ° C, reduce the reactor inlet oxygen content if desired to reduce any hot(test)-spot temperature.
(4) when exit gas reaches the inlet gas oxygen concentration of 70-80% once more, described bed inlet temperature is increased to 800/425 ° C, keep oxygen content in the inlet gas of 1 volume % simultaneously.At this moment, described regeneration should almost completely wherein significantly burnt above 90% coke, and temperature rise should be low.Do not allow any bed tempertaure to surpass 850/450 ° C, reduce the reactor inlet oxygen content if desired to reduce any hot(test)-spot temperature.
(5) when described exit gas reaches the inlet gas oxygen concentration of 90-100%; temperature is increased to 850/450 ° C; if fully purification of combustion be wish (this may be unnecessary; especially for large pore zeolite such as ZSM-12; β, modenites etc. are because significantly burned above 90% coke; and remaining coke can provide some to prevent the protection of steam inactivation and metal function sintering in a small amount), otherwise directly advance to next step.Should no longer include heat release this moment.The inlet oxygen content can further be increased to 7 volume %, and is complete to guarantee described calcination.In some embodiments, should not allow described bed tempertaure to surpass 850/450 ° C, and, reduce the reactor inlet oxygen content if desired, so that reduce any hot(test)-spot temperature for this purpose.
Described regeneration this moment is done, and temperature of reactor should be reduced to 600-700 °F, purges out oxygen with drying nitrogen, and carries out ready for operation for the starting order that is used for correlation technique according to catalyst will be fresh or that regenerate.
Importantly, described regeneration temperature low as far as possible (, only just increase temperature when (i.e. 70 volume %) break through in fact when oxygen, do not increase temperature before this) when coke is burned.Purpose is to remove most of coke under possible minimum temperature.Typically, in regeneration, in case oxygen begins to break through, the operator begins to raise temperature immediately with the highest burn rate of realization, and we have found that this makes described catalyst be exposed to more water under higher temperature.Although the inventive method needs long slightly calcination time, it is to carry out under lower mean temperature, has reduced inactivation, because temperature is an index to the influence of inactivation, and time effects is linear.Described new method also reduces the vapor partial pressure that described catalyst is run under higher temperature, because the coke of rich hydrogen be allowed to burn during at lower temperature early at described catalyst (particularly when described separator by often draining, if when being maintained at low temperature and using the recirculating gas gas dryer).
That summarize below is the result of the pilot-plant regeneration of aromatic compounds transalkylation catalyst (Pt-ZSM-12,0.1wt%Pt top bed and HZSM-5 bottom bed).As by as shown in processing performance and the catalyst characterization performance, the back two kinds of catalyst of the regeneration of about 32 weight % coke regain almost and the duplicate activity of fresh catalyst on catalyst.
Before the regeneration of TransPlus reactor and catalyst sorption capacity afterwards and activity (alpha test) be displayed in the following table 1.Described alpha test is described in United States Patent (USP) 3,354, and 078 and Journal of Catalysis, 4,527 (1965); 6,278 (1966); In 61,395 (1980).The experiment condition of described test used herein comprises steady temperature and the changeable flow of 538 ° of C, as at Journal of Catalysis, describes in detail in 61,395 (1980).Described test can be repeated to by those skilled in the art ± and 10%.
Table 1
Hexane absorbs according to United States Patent (USP) 6,048, and 816 and 6,046, the program determination described in 372.
In table 2, provided below before regeneration and the other characteristic of described catalyst afterwards.
Table 2
As described in can see that specificity of catalyst and processing performance confirm that all described renovation process successfully almost completely recovers fresh activity in the table.Almost the rate of ageing (about 3.6 ° of C/ months) with fresh catalyst is identical at described regeneration rear catalyst rate of ageing (about 3.4 ° of C/ months), and the recovery fully of metal function is also indicated in hydrogen consumption.Described catalyst ageing speed is indicated with the increase of keeping the desired temperature of constant conversion.
The order of step is important.Described O raise before the coke of burning appropriate amount at a lower temperature
2Concentration can cause too high bed tempertaure to change, and this promotes inactivation.
After explaining the present invention so in detail in conjunction with specific embodiments, grasp of the present disclosure those skilled in the art will recognize that, those skilled in the art can make various other and change under the situation that does not deviate from the spirit and scope of the present invention, and the present invention can be implemented in the mode that is different from the mask body elaboration.
In this article the trade name of Shi Yonging by
TMSymbol or
Symbol indicates, and represents that described title may be protected by some trade mark right, and for example they may be the registration marks in the various judicial powers.All patents quoted herein and patent application, test program and other file fully be incorporated herein by reference to so open not with the inconsistent degree of the present invention, and whole authorities that are allowed to for this introducing.Go up in limited time when listing digital lower limit and numeral in this article, the scope from any lower limit to any upper limit is expected.
Claims (9)
1. in the method for the zeolite catalyst that can be used for hydroconversion process that is used for regenerating, wherein said renovation process comprises the oxygen calcination to remove the coke that is deposited on the described catalyst in described hydroconversion process process, and improvement comprises:
(i) in comprising the fixed bed of described zeolite catalyst,, locate that measure, about 0.5 volume %O in gas access in described reactor beds under described reactor inlet place average reactor temperature that measure, that be not more than 370 ° of C
2Under the surplus inert gas atmosphere, beginning oxygen calcination, prerequisite is to select to comprise the condition of oxygen flow and gross pressure, makes along the temperature rise that not have on any point of described reactor beds above 55 ° of C; Then
The O that (ii) works as exit gas
2Content reaches about 70 volume % of described inlet gas content or when bigger, the inlet temperature of described bed is raised, and is not more than 400 ° of C but be increased to, and prerequisite is an alternative condition, makes along not having temperature to surpass 450 ° of C on any point of described reactor beds; Then
The O that (iii) works as exit gas
2Content reaches about 70 volume % of described inlet gas content or when bigger, the O of described inlet
2Content is raised to about 1.0 volume %, keeps described reactor inlet temperature to be not more than 400 ° of C simultaneously, and prerequisite is to select to comprise the condition of oxygen flow and gross pressure, makes along not having temperature to surpass 450 ° of C on any point of described reactor beds; Then
The O that (iv) works as exit gas
2Content reaches about 70 volume % of described inlet gas content or when bigger, the gas access temperature of described bed is raised, and is not more than 425 ° of C but be increased to, and keeps the O of described inlet simultaneously
2Content is at about 1.0 volume %, and prerequisite is to select to comprise the condition of oxygen flow and gross pressure, makes along not having temperature to surpass 450 ° of C on any point of described reactor beds; Then
(the O that v) works as exit gas
2Content reaches about 90 volume % of described inlet gas content or when bigger, the gas access temperature of described bed is raised, and is not more than 450 ° of C but be increased to, and keeps the O of described inlet simultaneously
2Content is at about 1.0 volume %, and prerequisite is to select to comprise the condition of oxygen flow and gross pressure, makes along not having temperature to surpass 450 ° of C on any point of described reactor beds; Then
(described inlet O vi) raises
2Content is to about 6-8 volume %, and prerequisite is to select to comprise the condition of oxygen flow and gross pressure, makes along not having temperature to surpass 450 ° of C on any point of described reactor beds; Then
(vii) reduce reactor inlet temperature to 370 ° C or lower, and remove O
2Charging makes described bed be under the inert atmosphere;
(viii) the progress of starting sequence that is used for described method according to catalyst fresh or regeneration carries out, and begins or continue described hydroconversion process.
2. the process of claim 1 wherein that described hydroconversion process comprises the first hydrocarbon feed stream and the fixed bde catalyst that comprises at least a zeolite contacting under the condition that is enough to transform described first feed stream to the second and different feed stream.
3. the method for claim 2, wherein said feed stream comprises non-aromatic hydrocarbon, aromatic hydrocarbon and contain in the one or more heteroatomic hydrocarbon that is selected from oxygen, sulphur, nitrogen and their mixture one or more.
4. each method in the aforementioned claim, wherein said hydroconversion process is selected from light olefin to the more conversion of higher alkene, oxygenate is to the conversion of gasoline, the hydration of methylated aromatic compounds to the disproportionation of dimethylbenzene and/or transalkylation and propylene to isopropyl alcohol and Di Iso Propyl Ether.
5. each method in the aforementioned claim, wherein said zeolite catalyst comprise and are selected from ZSM-5, β, ZSM-12, ZSM-23, the zeolite of one or more in the modenite.
6. each method in the aforementioned claim, wherein said zeolite catalyst also comprises one or more metals.
7. each method in the aforementioned claim, wherein said zeolite catalyst comprises at least a metal that is selected from platinum, palladium, rhodium and ruthenium.
8. each method in the aforementioned claim, wherein said zeolite catalyst comprises one or more metals that are selected from copper, silver, tin and their mixture.
9. each method in the aforementioned claim, wherein said fixed bed comprises first zeolite catalyst that contains first zeolite and randomly contain at least a metal, and comprise second zeolite and randomly contain second zeolite catalyst of at least a metal, with the kind of wherein said first zeolite catalyst at described zeolite, the perhaps existence of described metal or do not exist, perhaps if present in the kind aspect of described metal at least one aspect be different from described second zeolite catalyst.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US41821210P | 2010-11-30 | 2010-11-30 | |
| US61/418,212 | 2010-11-30 | ||
| PCT/US2011/056904 WO2012074613A1 (en) | 2010-11-30 | 2011-10-19 | Method of regenerating zeolite catalyst |
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| Publication Number | Publication Date |
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| CN103228357A true CN103228357A (en) | 2013-07-31 |
| CN103228357B CN103228357B (en) | 2016-03-23 |
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| CN201180057262.6A Active CN103228357B (en) | 2010-11-30 | 2011-10-19 | The method of regenerate zeolites catalyst |
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| WO (1) | WO2012074613A1 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014193563A1 (en) | 2013-05-31 | 2014-12-04 | Exxonmobil Chemical Patents Inc. | Transalkylation system |
| US9963403B2 (en) | 2014-10-27 | 2018-05-08 | Exxonmobil Chemical Patents Inc. | Process and apparatus for the conversion of hydrocarbons |
| US10450243B2 (en) | 2014-12-19 | 2019-10-22 | Exxonmobil Chemical Patents Inc. | Sulfiding process for aromatic transalkylations |
| CN112619629A (en) * | 2020-12-25 | 2021-04-09 | 青岛华世洁环保科技有限公司 | Runner regeneration method |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4300014A (en) * | 1980-08-04 | 1981-11-10 | Teijin Petrochemical Industries Ltd. | Process for isomerization of xylene |
| US4480144A (en) * | 1981-08-06 | 1984-10-30 | Mobil Oil Corporation | Regeneration of aromatics processing catalysts |
| US4876408A (en) * | 1986-12-19 | 1989-10-24 | Union Oil Company Of California | Alkylation process using a catalyst having an increased selectivity for monoalkylation |
| US6114265A (en) * | 1994-03-15 | 2000-09-05 | Exxon Research And Engineering Company | Combustion control in a fluid catalytic cracking regenerator |
| US6380119B1 (en) * | 1997-06-06 | 2002-04-30 | Basf Aktiengesellschaft | Method for regenerating a zeolitic catalyst |
| US20050075237A1 (en) * | 2003-10-03 | 2005-04-07 | Kelly Kevin P. | Alkylation and catalyst regenerative process |
| WO2009073263A1 (en) * | 2007-12-03 | 2009-06-11 | Uop Llc | Regeneration process for a c8 alkylaromatic isomerization catalyst |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3354078A (en) | 1965-02-04 | 1967-11-21 | Mobil Oil Corp | Catalytic conversion with a crystalline aluminosilicate activated with a metallic halide |
| US6046372A (en) | 1996-10-02 | 2000-04-04 | Mobil Oil Corporation | Process for producing light olefins |
| US6048816A (en) | 1996-10-02 | 2000-04-11 | Mobil Oil Corporation | Catalyst and process for converting methanol to hydrocarbons |
-
2011
- 2011-10-19 CN CN201180057262.6A patent/CN103228357B/en active Active
- 2011-10-19 WO PCT/US2011/056904 patent/WO2012074613A1/en active Application Filing
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4300014A (en) * | 1980-08-04 | 1981-11-10 | Teijin Petrochemical Industries Ltd. | Process for isomerization of xylene |
| US4480144A (en) * | 1981-08-06 | 1984-10-30 | Mobil Oil Corporation | Regeneration of aromatics processing catalysts |
| US4876408A (en) * | 1986-12-19 | 1989-10-24 | Union Oil Company Of California | Alkylation process using a catalyst having an increased selectivity for monoalkylation |
| US6114265A (en) * | 1994-03-15 | 2000-09-05 | Exxon Research And Engineering Company | Combustion control in a fluid catalytic cracking regenerator |
| US6380119B1 (en) * | 1997-06-06 | 2002-04-30 | Basf Aktiengesellschaft | Method for regenerating a zeolitic catalyst |
| US20050075237A1 (en) * | 2003-10-03 | 2005-04-07 | Kelly Kevin P. | Alkylation and catalyst regenerative process |
| WO2009073263A1 (en) * | 2007-12-03 | 2009-06-11 | Uop Llc | Regeneration process for a c8 alkylaromatic isomerization catalyst |
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| Publication number | Publication date |
|---|---|
| CN103228357B (en) | 2016-03-23 |
| WO2012074613A1 (en) | 2012-06-07 |
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