US20080058566A1 - Processes for reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst - Google Patents

Processes for reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst Download PDF

Info

Publication number
US20080058566A1
US20080058566A1 US11/515,679 US51567906A US2008058566A1 US 20080058566 A1 US20080058566 A1 US 20080058566A1 US 51567906 A US51567906 A US 51567906A US 2008058566 A1 US2008058566 A1 US 2008058566A1
Authority
US
United States
Prior art keywords
catalyst
alkylation
output stream
preliminary
sio
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US11/515,679
Other languages
English (en)
Inventor
James R. Butler
Xin Xiao
Jim Merrill
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Fina Technology Inc
Original Assignee
Fina Technology Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=39152703&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=US20080058566(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Fina Technology Inc filed Critical Fina Technology Inc
Priority to US11/515,679 priority Critical patent/US20080058566A1/en
Assigned to FINA TECHNOLOGY, INC. reassignment FINA TECHNOLOGY, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BUTLER, JAMES, MERRILL, JIM, XIAO, XIN
Priority to KR1020147005866A priority patent/KR101587786B1/ko
Priority to JP2009526843A priority patent/JP5486306B2/ja
Priority to CA2661021A priority patent/CA2661021C/fr
Priority to KR1020147005870A priority patent/KR101586629B1/ko
Priority to MX2009002350A priority patent/MX2009002350A/es
Priority to CN2011100463851A priority patent/CN102153435A/zh
Priority to KR1020097006770A priority patent/KR101542785B1/ko
Priority to EP07841389A priority patent/EP2064168A4/fr
Priority to CNA2007800324598A priority patent/CN101511753A/zh
Priority to PCT/US2007/076872 priority patent/WO2008030722A2/fr
Publication of US20080058566A1 publication Critical patent/US20080058566A1/en
Priority to US13/028,381 priority patent/US9375706B2/en
Priority to US13/212,234 priority patent/US9556083B2/en
Priority to US13/863,722 priority patent/US8552238B2/en
Priority to US14/014,098 priority patent/US8680354B2/en
Priority to US14/154,422 priority patent/US9556084B2/en
Priority to US14/929,744 priority patent/US20160052839A1/en
Abandoned legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
    • C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
    • C07C2/66—Catalytic processes
    • 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
    • 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
    • B01J29/7049—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
    • B01J29/7057—Zeolite Beta
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C15/00—Cyclic hydrocarbons containing only six-membered aromatic rings as cyclic parts
    • C07C15/02—Monocyclic hydrocarbons
    • C07C15/067—C8H10 hydrocarbons
    • C07C15/073—Ethylbenzene
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C6/00—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions
    • C07C6/08—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond
    • C07C6/12—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring
    • C07C6/126—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring of more than one hydrocarbon
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00004—Scale aspects
    • B01J2219/00006—Large-scale industrial plants
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

Definitions

  • Embodiments of the present invention generally relate to alkylation of aromatic compounds.
  • embodiments of the invention generally relate to reducing the deactivation of the alkylation catalyst within alkylation systems.
  • Alkylation reactions generally involve contacting a first aromatic compound with an alkylation catalyst to form a second aromatic compound.
  • alkylation catalysts generally experience deactivation requiring either regeneration or replacement. Some of the deactivation results from poisons present in the input stream to the alkylation system. Therefore, a need exists to develop an alkylation system that is capable of reducing alkylation catalyst deactivation.
  • Embodiments of the present invention include alkylation systems.
  • the alkylation systems generally include a preliminary alkylation system adapted to receive an input stream including an alkyl aromatic hydrocarbon and contact the input stream with a preliminary alkylation catalyst disposed therein to form a first output stream.
  • the preliminary alkylation catalyst generally includes a zeolite catalyst having a SiO 2 /Al 2 O 3 ratio of less than about 25.
  • the alkylation systems may further include a first alkylation system adapted to receive the first output stream and contact the first output stream with a first alkylation catalyst disposed therein and an alkylating agent to form a second output stream.
  • the alkylation system includes a preliminary alkylation catalyst having a first SiO 2 /Al 2 O 3 ratio and a first alkylation catalyst having a second SiO 2 /Al 2 O 3 ratio, wherein the first SiO 2 /Al 2 O 3 ratio is lower than the second SiO 2 /Al 2 O 3 ratio.
  • Embodiments further include methods of minimizing alkylation catalyst regeneration.
  • Such methods generally include substantially continuously introducing an alkyl aromatic hydrocarbon and an alkylating agent to an alkylation system having an alkylation catalyst disposed therein, contacting the input stream with the alkylation catalyst to form an output stream and withdrawing the output stream from the alkylation system over a period of time substantially equal to a life of the alkylation catalyst.
  • the methods further include contacting the input stream with a preliminary catalyst including a zeolite catalyst having a SiO 2 /Al 2 O 3 ratio of 25 or less prior to feeding the input stream to the alkylation system.
  • Such methods generally result in an alkylation catalyst life that is longer than the same alkylation catalyst's life in the absence of contact with the preliminary catalyst.
  • FIG. 1A illustrates an embodiment of an alkylation system.
  • FIG. 1B illustrates an embodiment of a separation system.
  • the term “activity” refers to the weight of product produced per weight of the catalyst used in a process per hour of reaction at a standard set of conditions (e.g., grams product/gram catalyst/hr).
  • alkylation refers to the addition of an alkyl group to another molecule.
  • deactivated catalyst refers to a catalyst that has lost enough catalyst activity to no longer be efficient in a specified process. Such efficiency is determined by individual process parameters. Further, the time from introduction of the catalyst to a system to the point that the catalyst is a deactivated catalyst is generally referred to as the catalyst life.
  • processing is not limiting and includes agitating, mixing, milling, blending and combinations thereof, all of which are used interchangeably herein. Unless otherwise specified, the processing may occur in one or more vessels, such vessels being known to one skilled in the art.
  • recycle refers to returning an output of a system as input to either that same system or another system within a process.
  • the output may be recycled to the system in any manner known to one skilled in the art, for example, by combining the output with an input stream or by directly feeding the output into the system.
  • multiple input/recycle streams may be fed to a system in any manner known to one skilled in the art.
  • regeneration refers to a process for renewing catalyst activity and/or making a catalyst reusable after its activity has reached an unacceptable/inefficient level. Examples of such regeneration may include passing steam over a catalyst bed or burning off carbon residue, for example.
  • molecular sieve refers to a material having a fixed, open-network structure, usually crystalline, that may be used to separate hydrocarbons or other mixtures by selective occlusion of one or more of the constituents, or may be used as a catalyst in a catalytic conversion process.
  • zeolite refers to a molecular sieve containing a silicate lattice, usually in association with some aluminum, boron, gallium, iron, and/or titanium, for example.
  • the terms molecular sieve and zeolite will be used more or less interchangeably.
  • teachings relating to zeolites are also applicable to the more general class of materials called molecular sieves.
  • FIG. 1 illustrates a schematic block diagram of an embodiment of an alkylation/transalkylation process 100 .
  • the process stream flow may be modified based on unit optimization so long as the modification complies with the spirit of the invention, as defined by the claims.
  • at least a portion of any overhead fraction may be recycled as input to any other system within the process and/or any process stream may be split into multiple process stream inputs, for example.
  • additional process equipment such as heat exchangers, may be employed in the processes described herein and such use is generally known to one skilled in the art.
  • the streams indicated below may include any additional components as known to one skilled in the art.
  • the process 100 generally includes supplying an input stream 102 (e.g., a first input stream) to an alkylation system 104 (e.g., a first alkylation system).
  • the alkylation system 104 is generally adapted to contact the input stream 102 with an alkylation catalyst to form an alkylation output stream 106 (e.g., a first output stream).
  • an additional input such as an alkylating agent, may be supplied to the alkylation system 104 via line 103 .
  • the separation system 107 generally includes a plurality of vessels, such vessels being adapted to separate components of the output stream 106 .
  • a separation system output 120 is passed from the separation system 107 to a second alkylation system 121 (e.g., a transalkylation system) as transalkylation input 120 .
  • an additional input such as additional aromatic compound, may be supplied to the second alkylation system 121 , which may alternatively be referred to as a transalkylation system, via line 122 to contact a transalkyation catalyst disposed therein and form a transalkylation output 124 .
  • the input stream 102 generally includes a first aromatic compound.
  • the aromatic compound may include substituted or unsubstituted aromatic compounds. If present, the substituents on the aromatic compounds may be independently selected from alkyl, aryl, alkaryl, alkoxy, aryloxy, cycloalkyl, halide and/or other groups that do not interfere with the alkylation reaction, for example.
  • substituted aromatic compounds generally include toluene, xylene, isopropylbenzene, normal propylbenzene, alpha-methylnaphthalene, ethylbenzene, mesitylene, durene, cymene, butylbenzene, pseudocumene, o-diethylbenzene, m-diethylbenzene, p-diethylbenzene, isoamylbenzene, isohexylbenzene, pentaethylbenzene, pentamethylbenzene, 1,2,3,4-tetraethylbenzene, 1,2,3,5-tetramethylbenzene, 1,2,4-triethylbenzene, 1,2,3-trimethylbenzene, m-butyltoluene, p-butyltoluene, 3,5-diethyltoluene, o-ethyltoluene, o
  • aromatic compounds include hexylbenzene, nonylbenzene, dodecylbenzene, pentadecylbenzene, hexyltoluene, nonyltoluene, dodecyltoluene and pentadecytoluene.
  • the aromatic compound includes one or more hydrocarbons, such as benzene, naphthalene, anthracene, naphthacene, perylene, coronene and phenanthrene, for example.
  • the first aromatic compound includes benzene.
  • the benzene may be supplied from a variety of sources, such as a fresh benzene source and/or a variety of recycle sources, for example.
  • fresh benzene source refers to a source including at least about 95 wt. % benzene, at least about 98 wt. % benzene or at least about 99 wt. % benzene, for example.
  • the alkylating agent may include olefins (e.g., ethylene, propylene, butene and pentene), alcohols (e.g., methanol, ethanol, propanol, butanol and pentanol), aldehydes (e.g., formaldehyde, acetaldehyde, propionaldehyde, butyraldehyde and n-valeraldehyde) and/or alkyl halides (e.g., methyl chloride, ethyl chloride, propyl chloride, butyl chloride and pentyl chloride), for example.
  • the alkylating agent includes a mixture of light olefins, such as mixtures of ethylene, propylene, butene and/or pentenes, for example.
  • the alkylating agent includes ethylene.
  • the input stream 102 and/or line 103 may further include other compounds in minor amounts (e.g., sometimes referred to as poisons or inactive compounds), such as C 7 aliphatic compounds and/or nonaromatic compounds, for example.
  • the input stream 102 includes less than about 3% of such compounds or less than about 1%, for example (e.g., about 100 ppb or less, or about 80 ppb or less or about 50 ppb or less).
  • the alkylation system 104 generally includes one or more reaction vessels.
  • the reaction vessels may include continuous flow reactors (e.g., fixed-bed, slurry bed or fluidized bed), for example.
  • the alkylation system 104 includes a plurality of multi-stage reaction vessels (not shown).
  • the plurality of multi-stage reaction vessels may include a plurality of operably connected catalyst beds, such beds containing an alkylation catalyst (not shown).
  • the number of catalyst beds is generally determined by individual process parameters, but may include from 2 to 20 catalyst beds or from 3 to 10 catalyst beds, for example.
  • Such reaction vessels may be liquid phase, vapor phase, supercritical phase or mixed phase reactors operated at reactor temperatures and pressures sufficient to maintain the alkylation reaction in the corresponding phase, i.e., the phase of the aromatic compound, for example.
  • Such temperatures and pressures are generally determined by individual process parameters.
  • the plurality of stages within a reaction vessel may be operated with the same or different catalyst and at the same or different temperatures and space velocities.
  • Such temperatures and pressures are generally determined by individual process parameters.
  • liquid phase reactions may occur at temperatures of from about 160° C. to about 270° C. and pressures of from about 400 psig to about 700 psig, for example.
  • Vapor phase reactions may occur at temperatures of from about 350° C. to about 500° C. and pressures of from about 200 psig to about 355 psig, for example.
  • the alkylation catalyst may include a molecular sieve catalyst.
  • Such molecular sieve catalyst may include zeolite beta, zeolite Y, 25M-5, zeolite MCM-22, zeolite MCM-36, zeolite MCM-49 or zeolite MCM-56, for example.
  • the catalyst is a zeolite beta having a silica to alumina molar ratio (expressed as SiO 2 /Al 2 O 3 ratio) of from about 5 to about 200 or from about 20 to about 100, for example.
  • the zeolite beta may have a low sodium content, e.g., less than about 0.2 wt.
  • the sodium content may be reduced by any method known to one skilled in the art, such as through ion exchange, for example.
  • ion exchange any method known to one skilled in the art, such as through ion exchange, for example.
  • U.S. Pat. No. 3,308,069 and U.S. Pat. No. 4,642,226 formation of zeolite beta
  • U.S. Pat. No. 4,185,040 formation of zeolite Y
  • U.S. Pat. No. 4,992,606 formation of MCM-22
  • U.S. Pat. No. 5,258,565 formation of MCM-36
  • WO 94/29245 formation of MCM-49
  • U.S. Pat. No. 5,453,554 formation of MCM-56
  • the alkylation catalyst includes a rare earth modified catalyst, such as a cerium promoted zeolite catalyst.
  • the cerium promoted zeolite catalyst is a cerium promoted zeolite beta catalyst.
  • the cerium promoted zeolite beta (e.g., cerium beta) catalyst may be formed from any zeolite catalyst known to one skilled in the art.
  • the cerium beta catalyst may include zeolite beta modified by the inclusion of cerium. Any method of modifying the zeolite beta catalyst with cerium may be used.
  • the zeolite beta may be formed by mildly agitating a reaction mixture including an alkyl metal halide and an organic templating agent (e.g., a material used to form the zeolite structure) for a time sufficient to crystallize the reaction mixture and form the zeolite beta (e.g., from about 1 day to many months via hydrothermal digestion), for example.
  • the alkyl metal halide may include silica, alumina, sodium or another alkyl metal oxide, for example.
  • the hydrothermal digestion may occur at temperatures of from slightly below the boiling point of water at atmospheric pressure to about 170° C. at pressures equal to or greater than the vapor pressure of water at the temperature involved, for example.
  • the cerium promoted zeolite beta may have a silica to alumina molar ratio (expressed as SiO 2 /Al 2 O 3 ratio) of from about 10 to about 200 or about 50 to 100, for example.
  • the alkylation catalyst may optionally be bound to, supported on or extruded with any support material.
  • the alkylation catalyst may be bound to a support to increase the catalyst strength and attrition resistance to degradation.
  • the support material may include alumina, silica, aluminosilicate, titanium and/or clay, for example.
  • the alkylation output 106 generally includes a second aromatic compound formed from the reaction of the first aromatic compound and the alkylating agent in the presence of the alkylation catalyst, for example.
  • the second aromatic compound includes ethylbenzene.
  • the transalkylation system 121 generally includes one or more reaction vessels having a transalkylation catalyst disposed therein.
  • the reaction vessels may include any reaction vessel, combination of reaction vessels and/or number of reaction vessels (either in parallel or in series) known to one skilled in the art.
  • Such temperatures and pressures are generally determined by individual process parameters.
  • liquid phase reactions may occur at temperatures of from about 65° C. to about 290° C. (e.g., the critical temperature of the first aromatic compound) and pressures of from about 800 psig or less, for example.
  • Vapor phase reactions may occur at temperatures of from about 350° C. to about 500° C. and pressures of from about 200 psi to about 500 psi, for example.
  • the transalkylation output 124 generally includes the second aromatic compound, for example.
  • any of the process streams, such as the transalkylation output 124 may be used for any suitable purpose or recycled back as input to another portion of the system 100 , such as the separation system 107 , for example.
  • the transalkylation catalyst may include a molecular sieve catalyst and may be the same catalyst or a different catalyst than the alkylation catalyst, for example.
  • Such molecular sieve catalyst may include zeolite beta, zeolite Y, zeolite MCM-22, zeolite MCM-36, zeolite MCM-49 or zeolite MCM-56, for example.
  • the first aromatic compound includes benzene and the first alkylating agent includes ethylene.
  • the molar ratio of benzene to ethylene entering the alkylation system 104 may be from about 1:1 to about 30:1, or from about 1:1 to about 20:1 or from about 5:1 to about 15:1 and the space velocity may be from about 2 to about 10, for example.
  • the separation system (or product recovery) 107 includes three separation zones (illustrated in FIG. 1B ) operated at conditions known to one skilled in the art.
  • the first separation zone 108 may include any process or combination of processes known to one skilled in the art for the separation of aromatic compounds.
  • the first separation zone 108 may include one or more distillation columns (not shown), either in series or in parallel. The number of such columns may depend on the volume of the alkylation output 106 passing therethrough, for example.
  • the overhead fraction 110 from the first column 108 generally includes the first aromatic compound, such as benzene, for example.
  • the bottoms fraction 112 from the first separation zone 108 generally includes the second aromatic compound, such as ethylbenzene, for example.
  • the bottoms fraction 112 further includes additional components, which may undergo further separation in the second separation zone 114 and third separation zone 115 , discussed further below.
  • the second separation zone 114 may include any process known to one skilled in the art, for example, one or more distillation columns (not shown), either in series or in parallel.
  • the overhead fraction 116 from the second separation zone 114 generally includes the second aromatic compound, such as ethylbenzene, which may be recovered and used for any suitable purpose, such as the production of styrene, for example.
  • the bottoms fraction 118 from the second separation zone 114 generally includes heavier aromatic compounds, such as polyethylbenzene, cumene and/or butylbenzene, for example, which may undergo further separation in the third separation zone 115 .
  • the third separation zone 115 generally includes any process known to one skilled in the art, for example, one or more distillation columns (not shown), either in series or in parallel.
  • the overhead fraction 120 from the third separation zone 115 may include diethylbenzene and liquid phase triethylbenzene, for example.
  • the bottoms fraction 119 (e.g., heavies) may be recovered from the third separation zone 115 for further processing and recovery (not shown).
  • alkylation and transalkylation catalysts generally experience deactivation upon exposure to reaction.
  • the deactivation results from a number of factors.
  • poisons present in the input stream 102 such as nitrogen, sulfur and/or oxygen containing impurities, either naturally occurring or a result of a prior process, may reduce the activity of the alkylation catalyst.
  • the alkylation/transalkylation system 100 further includes a preliminary alkylation system 200 .
  • the preliminary alkylation input stream 202 may be passed through the preliminary alkylation system 200 prior to entry into the alkylation system 104 to reduce the level of poisons in the input stream 102 , for example.
  • the level of poisons is reduced by at least 10%, or at least 20% or at least 30% or at least 40% or at least 50%, for example.
  • the preliminary alkylation system 200 may be maintained at ambient or up to alkylation conditions, for example.
  • the preliminary alkylation system 200 may be operated under liquid phase and/or vapor phase conditions.
  • the preliminary alkylation system 200 may be operated at a temperature of from about 20° C. to about 270° C. and a pressure of from about 675 kPa to about 8300 kPa.
  • the preliminary alkylation system 200 generally includes a preliminary alkylation catalyst disposed therein.
  • the alkylation catalyst, transalkylation catalyst and/or the preliminary catalyst may be the same or different.
  • such catalysts include molecular sieve catalysts, such as zeolite Y or zeolite beta catalysts, for example.
  • the preliminary catalyst in the preliminary alkylation system 200 has typically deactivated rapidly, requiring frequent regeneration and/or replacement.
  • the preliminary catalyst may experience deactivation more rapidly than the alkylation catalyst (e.g., from about twice as often to about 1.5 times as often).
  • Previous systems have generally used the preliminary alkylation system 200 as a sacrificial system, thereby reducing the amount of poisons contacting the alkylation catalyst in the alkylation system 104 .
  • embodiments of the invention utilize a catalyst having a lower SiO 2 /Al 2 O 3 ratio than those preliminary alkylation catalysts previously used (and discussed herein).
  • the preliminary alkylation catalyst may have a SiO 2 /Al 2 O 3 ratio that is about 50 or less, or that is about 25 or less, or that is from about 5 to about 50 or from about 7.5 to about 25, for example.
  • the preliminary alkylation catalyst has a SiO 2 /Al 2 O 3 ratio that is lower than the SiO 2 /Al 2 O 3 ratio of the alkylation catalyst.
  • the preliminary alkylation catalyst may have a SiO 2 /Al 2 O 3 ratio that is at least about 25%, or at least about 50%, or at least about 75% or at least about 90% lower than the SiO 2 /Al 2 O 3 ratio of the alkylation catalyst.
  • the preliminary alkylation catalyst may include any commercially available catalyst having the SiO 2 /Al 2 O 3 ratio discussed herein.
  • the preliminary alkylation catalyst may include Y-84 zeolite (i.e., SiO 2 /Al 2 O 3 ratio of 9.1), for example.
  • the preliminary alkylation catalyst may include a plurality of preliminary alkylation catalysts so long as at least one of the plurality of preliminary alkylation catalysts include the lower SiO 2 /Al 2 O 3 ratio preliminary alkylation catalyst described herein.
  • the regeneration procedure may includes processing the deactivated catalyst at high temperatures, although the regeneration may include any regeneration procedure known to one skilled in the art.
  • Off-stream reactor purging may be performed by contacting the catalyst in the off-line reactor with a purging stream, which may include any suitable inert gas (e.g., nitrogen), for example.
  • a purging stream which may include any suitable inert gas (e.g., nitrogen), for example.
  • the off-stream reactor purging conditions are generally determined by individual process parameters and are generally known to one skilled in the art.
  • the catalyst may then undergo regeneration.
  • the regeneration conditions may be any conditions that are effective for at least partially reactivating the catalyst and are generally known to one skilled in the art.
  • regeneration may include heating the catalyst to a temperature or a series of temperatures, such as a regeneration temperature of from about 50° C. to about 400° C. above the purging or reaction temperature, for example.
  • the alkylation catalyst is heated to a first temperature (e.g., 700° F.) with a gas containing nitrogen and about 2% oxygen, for example, for a time sufficient to provide an output stream having an oxygen content of about 0.5%.
  • the catalyst may then be heated to a second temperature for a time sufficient to provide an output stream having an oxygen content of about 2.0%.
  • the second temperature may be about 50° F. greater than the first temperature, for example.
  • the second temperature is generally about 950° F. or less, for example.
  • the catalyst may further be held at the second temperature for a period of time, or at a third temperature that is greater than the second temperature, for example.
  • the catalyst may then be reused for alkylation and transalkylation, for example.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Materials Engineering (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Catalysts (AREA)
US11/515,679 2006-09-05 2006-09-05 Processes for reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst Abandoned US20080058566A1 (en)

Priority Applications (17)

Application Number Priority Date Filing Date Title
US11/515,679 US20080058566A1 (en) 2006-09-05 2006-09-05 Processes for reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst
CNA2007800324598A CN101511753A (zh) 2006-09-05 2007-08-27 使用低氧化硅与氧化铝比例减轻烷基化催化剂失活的方法
PCT/US2007/076872 WO2008030722A2 (fr) 2006-09-05 2007-08-27 Procédés de réduction de la désactivation d'un catalyseur d'alkylation
CN2011100463851A CN102153435A (zh) 2006-09-05 2007-08-27 使用低氧化硅与氧化铝比例减轻烷基化催化剂失活的方法
EP07841389A EP2064168A4 (fr) 2006-09-05 2007-08-27 Procédés de réduction de la désactivation d'un catalyseur d'alkylation
JP2009526843A JP5486306B2 (ja) 2006-09-05 2007-08-27 低いシリカ対アルミナ比の触媒を使用する、アルキル化触媒の失活の減少法
CA2661021A CA2661021C (fr) 2006-09-05 2007-08-27 Procedes de reduction de la desactivation d'un catalyseur d'alkylation
KR1020147005870A KR101586629B1 (ko) 2006-09-05 2007-08-27 알킬 방향족 화합물 제조방법
MX2009002350A MX2009002350A (es) 2006-09-05 2007-08-27 Procesos para la reduccion de desactivacion del catalizador de alquilacion utilizando catalizador de baja relación de silice a alumina.
KR1020147005866A KR101587786B1 (ko) 2006-09-05 2007-08-27 알킬화 촉매 재생을 최소화시키는 방법
KR1020097006770A KR101542785B1 (ko) 2006-09-05 2007-08-27 저 실리카 대 알루미나 비의 촉매를 사용하여 알킬화 촉매 불활성화를 감소시키기 위한 방법
US13/028,381 US9375706B2 (en) 2006-09-05 2011-02-16 Use of swing preliminary alkylation reactors
US13/212,234 US9556083B2 (en) 2006-09-05 2011-08-18 Processes for the reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst
US13/863,722 US8552238B2 (en) 2006-09-05 2013-04-16 Process for the reduction of alkylation catalyst deactivation
US14/014,098 US8680354B2 (en) 2006-09-05 2013-08-29 Process for the reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst
US14/154,422 US9556084B2 (en) 2006-09-05 2014-01-14 Process for the reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst
US14/929,744 US20160052839A1 (en) 2006-09-05 2015-11-02 Use of Swing Preliminary Alkylation Reactors

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US11/515,679 US20080058566A1 (en) 2006-09-05 2006-09-05 Processes for reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst

Related Child Applications (2)

Application Number Title Priority Date Filing Date
US13/028,381 Continuation-In-Part US9375706B2 (en) 2006-09-05 2011-02-16 Use of swing preliminary alkylation reactors
US13/212,234 Continuation US9556083B2 (en) 2006-09-05 2011-08-18 Processes for the reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst

Publications (1)

Publication Number Publication Date
US20080058566A1 true US20080058566A1 (en) 2008-03-06

Family

ID=39152703

Family Applications (5)

Application Number Title Priority Date Filing Date
US11/515,679 Abandoned US20080058566A1 (en) 2006-09-05 2006-09-05 Processes for reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst
US13/212,234 Active US9556083B2 (en) 2006-09-05 2011-08-18 Processes for the reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst
US13/863,722 Active US8552238B2 (en) 2006-09-05 2013-04-16 Process for the reduction of alkylation catalyst deactivation
US14/014,098 Active US8680354B2 (en) 2006-09-05 2013-08-29 Process for the reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst
US14/154,422 Active 2026-09-16 US9556084B2 (en) 2006-09-05 2014-01-14 Process for the reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst

Family Applications After (4)

Application Number Title Priority Date Filing Date
US13/212,234 Active US9556083B2 (en) 2006-09-05 2011-08-18 Processes for the reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst
US13/863,722 Active US8552238B2 (en) 2006-09-05 2013-04-16 Process for the reduction of alkylation catalyst deactivation
US14/014,098 Active US8680354B2 (en) 2006-09-05 2013-08-29 Process for the reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst
US14/154,422 Active 2026-09-16 US9556084B2 (en) 2006-09-05 2014-01-14 Process for the reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst

Country Status (8)

Country Link
US (5) US20080058566A1 (fr)
EP (1) EP2064168A4 (fr)
JP (1) JP5486306B2 (fr)
KR (3) KR101542785B1 (fr)
CN (2) CN101511753A (fr)
CA (1) CA2661021C (fr)
MX (1) MX2009002350A (fr)
WO (1) WO2008030722A2 (fr)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100060877A1 (en) * 2004-06-07 2010-03-11 Nikon Corporation Stage unit, exposure apparatus, and exposure method
US20100081856A1 (en) * 2008-09-30 2010-04-01 Fina Technology, Inc. Process for Ethylbenzene Production
EP2252566A2 (fr) * 2008-03-13 2010-11-24 Fina Technology, Inc. Procédé d alkylation en phase liquide
US20110020571A1 (en) * 2009-07-24 2011-01-27 Fina Technology, Inc. Polystyrene Nanocomposites for Blow Molding Applications
WO2011146187A3 (fr) * 2010-05-20 2012-02-09 Exxonmobil Chemical Patents Inc. Procédé d'alkylation amélioré
US8455383B2 (en) 2009-09-28 2013-06-04 Fina Technology, Inc. Process for catalyst regeneration and extended use
WO2013162626A1 (fr) * 2012-04-27 2013-10-31 Fina Technology, Inc. Addition d'une base pour améliorer le rendement de produit dans des réactions d'alkylation
WO2013162627A1 (fr) * 2012-04-27 2013-10-31 Fina Technology , Inc. Addition d'azote basique à des réactions d'alkylation
US20190016647A1 (en) * 2016-02-17 2019-01-17 Badger Licensing Llc Process for producing ethylbenzene

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7645913B2 (en) 2007-01-19 2010-01-12 Exxonmobil Chemical Patents Inc. Liquid phase alkylation with multiple catalysts
CN105709815B (zh) * 2014-12-02 2018-06-19 中国石油化工股份有限公司 一种甲苯与乙烯选择性烷基化催化剂及其制备方法
KR102235874B1 (ko) 2016-10-06 2021-04-06 엑손모빌 케미칼 패턴츠 인코포레이티드 벤젠 및/또는 톨루엔의 메틸화에 의해 파라크실렌을 생성시키기 위한 촉매의 선택화 방법
CN109963828A (zh) * 2016-10-06 2019-07-02 埃克森美孚化学专利公司 芳族烃的甲基化方法
CN110035987B (zh) 2016-10-06 2022-04-19 埃克森美孚化学专利公司 通过苯和/或甲苯的甲基化生产对二甲苯的方法
US11673849B2 (en) 2016-12-21 2023-06-13 Exxonmobil Chemical Patents Inc. Process for selectivating catalyst for producing paraxylene by methylation of benzene and/or toluene

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4358362A (en) * 1981-01-15 1982-11-09 Mobil Oil Corporation Method for enhancing catalytic activity
US5081323A (en) * 1987-12-17 1992-01-14 Chevron Research And Technology Company Liquid phase alkylation or transalkylation process using zeolite beta
US5535817A (en) * 1989-07-28 1996-07-16 Uop Sorption cooling process and apparatus
US6297417B1 (en) * 1996-08-20 2001-10-02 The Dow Chemical Company Alkylation/transalkylation process with pretreatment of the alkylation/transalkylation feedstock
US20030149324A1 (en) * 2000-08-16 2003-08-07 Venkat Chaya R. Removal of polar contaminants from aromatic feedstocks
US20040068151A1 (en) * 2002-10-04 2004-04-08 Kelly Kevin P. Critical phase alkylation process
US20040192985A1 (en) * 2003-03-24 2004-09-30 Smith Charles Morris Feed pretreating
US20050143612A1 (en) * 2002-02-28 2005-06-30 Shyh-Yuan Hwang Production of alkyl aromatic compounds
US20060194991A1 (en) * 2005-02-25 2006-08-31 Fina Technology, Inc. Treatment of alkylation catalyst poisons
US7645913B2 (en) * 2007-01-19 2010-01-12 Exxonmobil Chemical Patents Inc. Liquid phase alkylation with multiple catalysts

Family Cites Families (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3308069A (en) 1964-05-01 1967-03-07 Mobil Oil Corp Catalytic composition of a crystalline zeolite
US4185040A (en) 1977-12-16 1980-01-22 Union Oil Company Of California Alkylation of aromatic hydrocarbons
US4642226A (en) 1984-04-16 1987-02-10 Mobil Oil Corporation Process for the preparation of zeolite Beta using dibenzyldimethylammonium ions and the product produced
US4992606A (en) 1988-10-06 1991-02-12 Mobil Oil Corp. Process for preparing short chain alkyl aromatic compounds
US5334795A (en) * 1990-06-28 1994-08-02 Mobil Oil Corp. Production of ethylbenzene
US5258565A (en) 1992-05-04 1993-11-02 Mobil Oil Corp. Process for preparing short chain alkylaromatic compounds
US5362697A (en) 1993-04-26 1994-11-08 Mobil Oil Corp. Synthetic layered MCM-56, its synthesis and use
EP0703887A1 (fr) 1993-06-16 1996-04-03 Mobil Oil Corporation Synthese de la phase liquide de l'ethylbenzene
US6002057A (en) * 1996-09-06 1999-12-14 Exxon Chemical Patents Inc. Alkylation process using zeolite beta
US5998687A (en) * 1997-07-29 1999-12-07 Uop Llc Ethylbenzene process using stacked reactor loading of beta and Y zeolites
US6057485A (en) * 1998-11-17 2000-05-02 Fina Technology, Inc. Gas phase alkylation with split load of catalyst
US20020042548A1 (en) * 2001-07-11 2002-04-11 Dandekar Ajit B. Process for producing cumene
FR2832144B1 (fr) * 2001-11-15 2004-09-24 Inst Francais Du Petrole Procede de production de phenylalcanes utilisant une combinaison de deux catalyseurs
US20040138511A1 (en) * 2003-01-10 2004-07-15 James Butler Aromatic alkylation process with direct recycle
US6894201B1 (en) * 2003-12-19 2005-05-17 Uop Llc Process and apparatus for the removal of nitrogen compounds from a fluid stream
US20060192985A1 (en) 2005-02-25 2006-08-31 Konica Minolta Systems Laboratory, Inc. Printing system
US7476774B2 (en) * 2005-02-28 2009-01-13 Exxonmobil Research And Engineering Company Liquid phase aromatics alkylation process
US7501547B2 (en) * 2006-05-10 2009-03-10 Exxonmobil Chemical Patents Inc. Alkylaromatics production

Patent Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4358362A (en) * 1981-01-15 1982-11-09 Mobil Oil Corporation Method for enhancing catalytic activity
US5081323A (en) * 1987-12-17 1992-01-14 Chevron Research And Technology Company Liquid phase alkylation or transalkylation process using zeolite beta
US5535817A (en) * 1989-07-28 1996-07-16 Uop Sorption cooling process and apparatus
US6297417B1 (en) * 1996-08-20 2001-10-02 The Dow Chemical Company Alkylation/transalkylation process with pretreatment of the alkylation/transalkylation feedstock
US20030149324A1 (en) * 2000-08-16 2003-08-07 Venkat Chaya R. Removal of polar contaminants from aromatic feedstocks
US6617482B1 (en) * 2000-08-16 2003-09-09 Exxonmobil Chemical Patents Inc. Removable of polar contaminants from aromatic feedstocks
US20050143612A1 (en) * 2002-02-28 2005-06-30 Shyh-Yuan Hwang Production of alkyl aromatic compounds
US20100268008A1 (en) * 2002-02-28 2010-10-21 Shyh-Yuan Hwang Production of alkyl aromatic compounds
US20040068151A1 (en) * 2002-10-04 2004-04-08 Kelly Kevin P. Critical phase alkylation process
US20040192985A1 (en) * 2003-03-24 2004-09-30 Smith Charles Morris Feed pretreating
US20060194991A1 (en) * 2005-02-25 2006-08-31 Fina Technology, Inc. Treatment of alkylation catalyst poisons
US7645913B2 (en) * 2007-01-19 2010-01-12 Exxonmobil Chemical Patents Inc. Liquid phase alkylation with multiple catalysts
US7777087B2 (en) * 2007-01-19 2010-08-17 Exxonmobil Chemical Patents Inc. Liquid phase alkylation with multiple catalysts

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100060877A1 (en) * 2004-06-07 2010-03-11 Nikon Corporation Stage unit, exposure apparatus, and exposure method
EP2252566A2 (fr) * 2008-03-13 2010-11-24 Fina Technology, Inc. Procédé d alkylation en phase liquide
EP2252566A4 (fr) * 2008-03-13 2012-04-18 Fina Technology Procédé d alkylation en phase liquide
US20100081856A1 (en) * 2008-09-30 2010-04-01 Fina Technology, Inc. Process for Ethylbenzene Production
US8865958B2 (en) 2008-09-30 2014-10-21 Fina Technology, Inc. Process for ethylbenzene production
US8697208B2 (en) 2009-07-24 2014-04-15 Fina Technology, Inc. Polystyrene nanocomposites for blow molding applications
US20110020571A1 (en) * 2009-07-24 2011-01-27 Fina Technology, Inc. Polystyrene Nanocomposites for Blow Molding Applications
US8455383B2 (en) 2009-09-28 2013-06-04 Fina Technology, Inc. Process for catalyst regeneration and extended use
US8993820B2 (en) 2010-05-20 2015-03-31 Exxonmobil Chemical Patents Inc. Alkylation process
US20130211164A1 (en) * 2010-05-20 2013-08-15 Matthew J. Vincent Alkylation Process
WO2011146189A3 (fr) * 2010-05-20 2012-04-19 Exxonmobil Chemical Patents Inc. Procédé d'alkylation amélioré
WO2011146187A3 (fr) * 2010-05-20 2012-02-09 Exxonmobil Chemical Patents Inc. Procédé d'alkylation amélioré
US9249067B2 (en) * 2010-05-20 2016-02-02 Exxonmobil Chemical Patents Inc. Alkylation process
US9382170B1 (en) * 2010-05-20 2016-07-05 Exxonmobil Chemical Patents Inc. Alkylation process
US8785706B2 (en) 2011-05-22 2014-07-22 Fina Technology, Inc. Addition of a base to enhance product yield in alkylation reactions
US20140256537A1 (en) * 2011-05-22 2014-09-11 Fina Technology, Inc. Addition of a Base to Enhance Product Yield in Alkylation Reactions
WO2013162626A1 (fr) * 2012-04-27 2013-10-31 Fina Technology, Inc. Addition d'une base pour améliorer le rendement de produit dans des réactions d'alkylation
WO2013162627A1 (fr) * 2012-04-27 2013-10-31 Fina Technology , Inc. Addition d'azote basique à des réactions d'alkylation
US20190016647A1 (en) * 2016-02-17 2019-01-17 Badger Licensing Llc Process for producing ethylbenzene
US10899683B2 (en) * 2016-02-17 2021-01-26 Badger Licensing Llc Process for producing ethylbenzene

Also Published As

Publication number Publication date
US8680354B2 (en) 2014-03-25
US8552238B2 (en) 2013-10-08
MX2009002350A (es) 2009-03-23
KR101542785B1 (ko) 2015-08-07
EP2064168A4 (fr) 2010-12-15
CN101511753A (zh) 2009-08-19
US20110301396A1 (en) 2011-12-08
US20130225888A1 (en) 2013-08-29
CA2661021C (fr) 2015-11-24
US9556084B2 (en) 2017-01-31
KR20140051390A (ko) 2014-04-30
WO2008030722A3 (fr) 2008-04-24
WO2008030722A2 (fr) 2008-03-13
JP5486306B2 (ja) 2014-05-07
CA2661021A1 (fr) 2008-03-13
JP2010502636A (ja) 2010-01-28
EP2064168A2 (fr) 2009-06-03
US20140005454A1 (en) 2014-01-02
KR101586629B1 (ko) 2016-01-19
KR20090059139A (ko) 2009-06-10
US9556083B2 (en) 2017-01-31
KR101587786B1 (ko) 2016-01-25
KR20140051389A (ko) 2014-04-30
CN102153435A (zh) 2011-08-17
US20140128651A1 (en) 2014-05-08

Similar Documents

Publication Publication Date Title
US9556084B2 (en) Process for the reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst
US8637720B2 (en) Processes for the reduction of alkylation catalyst deactivation utilizing stacked catalyst bed
US7495139B2 (en) Use of modified zeolite catalysts in alkylation systems
US20070161835A1 (en) Liquid phase alkylation system
US7569741B2 (en) Petrochemical feedstock purification
US20070161837A1 (en) Zeolitic transalkylation with aluminum chloride alkylation
US9375706B2 (en) Use of swing preliminary alkylation reactors

Legal Events

Date Code Title Description
AS Assignment

Owner name: FINA TECHNOLOGY, INC., TEXAS

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:BUTLER, JAMES;XIAO, XIN;MERRILL, JIM;REEL/FRAME:018280/0410

Effective date: 20060822

STCB Information on status: application discontinuation

Free format text: EXPRESSLY ABANDONED -- DURING EXAMINATION