Abstract: A method is disclosed combining the process for the hydration or etherification of light linear olefins, such as the production of diisopropyl ether (DIPE), with the process for the etherification of C.sub.4 + or C.sub.4 hydrocarbons containing isobutylene to produce alkyl tertiary butyl ether or ether-rich gasoline in a manner which effectively dewaters alkanol using the iso-olefin hydrocarbon feedstream as extractant. The combined process leads to the production of isopropyl tert-alkyl ethers. In the integrated process the high octane ethers produced may include methyl tert-butyl ether, methyl tert-amyl ether, isopropyl tert-butyl ether and diisopropyl ether. The process also results in the production of a gasoline stream rich in high octane ethers.

Abstract: A process for controlled, multi-stage regeneration of FCC catalyst is disclosed. A modified high efficiency catalyst regenerator, with a fast fluidized bed coke combustor, dilute phase transport riser, and second fluidized bed regenerates the catalyst in at least two stages. The primary stage of regeneration is in the coke combustor, at full CO oxidation conditions. The second stage of catalyst regeneration occurs in the second fluidized bed, at partial CO combustion conditions. The process permits regeneration of spent FCC catalyst while minimizing NOx exmissions and achieving significant reduction of SOx.

Abstract: An improved extraction and reactor system for reacting crude aqueous alcohol feedstock with iso-olefinic hydrocarbons to produce tertiary-alkyl ethers. This system is useful in extracting crude methanol in MTBE production.

Abstract: A catalytic cracking catalyst and process are disclosed using a catalyst containing: a matrix, a large pore molecular sieve, a shape selective paraffin cracking/isomerization zeolite and a shape selective aliphatic aromatization zeolite. An exemplary catalyst comprises dealuminized zeolite Y, optionally containing rare earth elements, HZSM-5, and gallium ZSM-5 in a matrix. The matrix contains and protects the relatively fragile zeolite components and acts as a sodium and metals sink. The large pore molecular sieve cracks large hydrocarbons to lighter paraffins and olefins. The shape selective paraffin cracking/isomerization component cracks/isomerizes the paraffins produced by the large pore molecular seive. The shape selective aliphatic aromatization catalyst converts light paraffins and olefins into aromatics. A single shape selective zeolite, e.g., ZSM-5 with a controlled amount of an aromatization component such as gallium, may promote both paraffin cracking/isomerization and aromatization.

Abstract: A process for regenerating solid particulate catalyst used in fixed bed hydrocarbon conversion processes, such as the shape selective zeolite conversion of olefins to gasoline and diesel fuel. Regeneration is achieved using a portion of a flue gas stream to regenerate catalyst and preheat feedstock. Economies in equipment and operation are realized by employing a once-through configuration for the regenerator gas stream.

Abstract: An integrated process is disclosed that substantially reduces the cost of producing MTBE and other alkyl tert-alkyl ethers by eliminating a major portion of the equipment and operating costs associated with the downstream processing of the etherification reactor effluent. The integrated process combines the process for the etherification of isoolefins and methanol, or other alkanols, to produce methyl tertiary alkyl ethers such as MTBE and/or TAME with the catalytic process for converting feedstock such as oxygenates, light olefins and paraffins to higher molecular weight hydrocarbons. Unconverted reactants from the etherification reaction, which may comprise unreacted alkanol and unreacted hydrocarbons or just unreacted hydrocarbons, are separated from the product ethers and passed to the catalytic conversion process reactor for conversion to gasoline boiling range hydrocarbons.

Abstract: A fluidized catalytic cracking process operates with a hot stripper to improve stripping of spent catalyst from the FCC process. The catalyst from the hot stripper is cooled by direct contact heat exchange with a source or cooled regenerated catalyst. Cooled catalyst may contact hot, stripped catalyst in the base of the stripper or downstream of the stripper. The cooled, stripped catalyst has reduced hydrogen, sulfur and coke content, improves regeneration efficiency, and reduces hydrothermal degradation of catalyst.

Abstract: The benzene concentration in the gasoline pool of a petroleum refinery is decreased by alkylation of the benzene in a catalytic dewaxing reactor using the olefinic by-products from the dewaxing reaction as alkylating agents. The catalytic dewaxing is preferably carried out in the presence of an intermediate pore size zeolite such as ZSM-5 using a distillate or lube boiling range dewaxing feed. The benzene rich feed preferably contains less than about 2% C.sub.7+ aromatics in order to reduce alkylation of non-objectionable species in the reformate.

Abstract: A petroleum refinery process for the production of alkyl aromatic hydrocarbons from a C.sub.4.sup.- fuel gas containing light olefins including ethene and propene and catalytic reformate containing C.sub.6 to C.sub.8 aromatics. The C.sub.4.sup.- fuel gas is contacted with the catalytic reformate at a weight ratio of aromatics to olefins of 10:1 to 15:1 over a zeolite catalyst under process conditions to alkylate the C.sub.6 to C.sub.8 aromatics, particularly benzene, in the reformate with ethene and propene in the C.sub.4.sup.- fuel gas to form alkyl aromatic hydrocarbons. The reaction is carried out in a riser reactor having multiple olefin feed injection points in the riser section of the reactor.The catalytic reaction also causes the conversion of a small amount of light olefins in the fuel gas to coke by-product and the deposition of coke on the catalyst. The deposited coke causes the partial deactivation of the catalyst.

Abstract: Gasoline octane number and yield are improved while excess fuel gas production is decreased in a catalytic cracking process by integrating etherification and oxygenate/aliphatic upgrading processes into the catalytic cracking unit product fractionation section.

Abstract: A fluid catalytic cracking (FCC) process and apparatus which employs relatively more elutriatable catalyst particles comprising intermediate pore zeolite, particularly ZSM-5, and relatively less elutriatable catalyst particles comprising large pore zeolite, preferably zeolite Y. The process and apparatus employ a first stripping vessel which also separates a more elutriatable first portion of catalyst from a less elutriatable second portion of catalyst. The more elutriatable first portion passes to a second stripping vessel, and subsequently recycles to a fluid catalytic cracking reactor riser. The second portion of less elutriatable catalyst passes from the first stripping vessel to a fluid catalytic cracking regenerator vessel and, after being regenerated, recycles to the reactor riser. The more elutriatable first portion contains a higher ratio of intermediate pore catalyst particles to large pore catalyst particles than does the second portion.

Abstract: Isopentene, or isoamylene, conversion to methyl tert-amyl ether can be substantially improved while high conversion of isobutylene to methyl tert-butyl ether can be maintained by carrying out the overall etherification process with alkanol in a staged manner, wherein the first stage is methanol etherification of a C.sub.5 +, or C.sub.5, hydrocarbon feedstream rich in isoamylene and the second stage is etherification to produce MTBE and additional TAME from a C.sub.4 +, or C.sub.4, feedstream. Unreacted methanol and hydrocarbons from the first etherification are uniquely separated by fractionation from the TAME product by using the second stage C.sub.4 + feedstream as a reflux stream to the fractionator and passed to the second etherification zone. Products from the second etherification zone are separated by distillation to produce MTBE, TAME and C.sub.5 +, or C.sub.5, hydrocarbons as a bottom stream.

Abstract: A catalytic cracking catalyst mixture and process are disclosed. The mixture comprises (a) a cracking catalyst containing a matrix and a large pore molecular sieve and (b) separate particles of additive catalyst comprising at least one of a shape selective paraffin cracking/isomerization zeolite and a shape selective aliphatic aromatization zeolite. An exemplary catalyst mixture comprises dealuminized zeolite Y, optionally containing rare earth elements, in an alumina rich matrix and an additive catalyst of HZSM-5, and gallium ZSM-5 in a matrix. The alumina matrix of the cracking catalyst acts as a sodium and metals sink. The large pore molecular sieve catalyst cracks large hydrocarbons to lighter paraffins and olefins. The shape selective paraffin cracking/isomerization component cracks the paraffins produced by the large pore molecular sieve. The shape selective aliphatic aromatization catalyst converts light paraffins and olefins into aromatics. A single shape selective zeolite, e.g.

Abstract: A process is disclosed for dewaxing a waxy hydrocarbon feedstock and for upgrading the olefinic interstage by-product to a high-octane gasoline blending stream. Waxy hydrocarbon feedstock is catalytically dewaxed until the catalyst is deactivated. Hydrogen-rich gas or, optionally, oxygen-containing gas, is then circulated to at least partially reactivate the catalyst. The interstage by-product, stored during the dewaxing run, is then upgraded in the reaction zone to a high-octane gasoline blending component.

Abstract: Methanol or other alcohol is converted to high octane gasoline components by an integrated process wherein crude aqueous alcohol feedstock is extracted with a liquid extractant stream containing C.sub.4.sup.+ iso-olefin and reacted to form tertiary-alkyl ethers, such as MTBE. The aqueous raffinate is converted to predominantly gasoline range liquid hydrocarbons in a MTG catalytic reactor, with byproduct alkanes rich in propane and isobutane. Dehydrogenation of C.sub.3 -C.sub.5 alkanes from the MTG unit provides propene and isobutene reactants for subsequent etherification steps. Propene from the MTG dehydrogenation step is reacted with water to produce di-isopropyl ether, which may be blended with MTBE and C.sub.6.sup.+ MTG hydrocarbons to produce high octane gasoline. Isobutylene and isoamylenes from the MTG dehydrogenation step can be removed and recycled as a liquid extractant stream.

Abstract: A process and apparatus for preheating and catalytic cracking of heavy oils is disclosed. Direct contact heat exchange of heavy feed, such as a resid, with hot product vapor from the cracking reactor provides an efficient way to preheat a heavy feed to an unusually high temperature, preferably in excess of 600.degree. F. Cooling hot cracked products from an FCC or TCC reactor upstream of the main fractionator reduces thermal cracking in the transfer line. High temperature preheat reduces the viscosity of the heavy feed, improves contact of heavy feed with cracking catalyst and reduces the amount of catalyst required to effect the catalytic cracking reaction. This improves yields, permits higher cracking reactor temperatures, and reduces cat:oil coke make.

Abstract: A process is disclosed for the production of high octane gasoline rich in aromatics but containing a relatively low concentration of benzene. The process comprises the separation of C.sub.6 fraction of the gasoline feedstock into n-hexane and C.sub.6 isomers. The n-hexane and C.sub.7 + streams are catalytically reformed to produce a reformate with a diminished yield of benzene. The reformate is separated and the C.sub.6 - reformate fraction containing benzene is alkylated employing acidic metallosilicate catalyst such as ZSM-5 as the catalyst and preferably methano or propylene as the alkylating agent. The alkylate comprises C.sub.7+ alkylaromatics. The C.sub.6 isomers are blended into the gasoline pool.

Abstract: A technique for converting olefinic light hydrocarbons to ether-rich liquid fuels and olefinic gasoline including etherification, olefin upgrading and transhydrogenation operations. The preferred process includes: reacting a fresh hydrocarbon stream containing C.sub.4 + iso-alkene with lower aliphatic alcohol in an etherification zone in contact with an acidic etherification catalyst under etherification conditions whereby an effluent stream containing C5+ tertiary-alkyl ether is produced; separating the etherification effluent stream to provide a first liquid stream comprising C5+ ether and a second stream comprising unreacted alcohol and C4+ hydrocarbons; contacting the second stream with acidic metallosilicate catalyst for conversion of oxygenates and olefins under olefin oligomerization and isomerization conditions at elevated temperature; separating oligomerization effluent to recover an intermediate hydrocarbon stream rich in C.sub.

Abstract: A reactor system contained in a fired heater and a hydrocarbon upgrading process are discosed for the concurrent conversion of a hydrocarbon feedstock and the regeneration of a deactivated catalyst. An effluent product slipstream from a set of operating reactors is used to hydrogen-regenerate deactivated catalyst in another set of reactors. Flue gas withdrawn from the fired heater stack is used as a purge and/or carrier gas during oxygen-regeneration of the catalyst.

Abstract: A fluid catalytic cracking process and apparatus is described which includes a high temperature stripper (hot stripper) to control the carbon level and sulfur on spent catalyst, followed by catalyst cooling to control the regeneration inlet temperature. The high temperature stripper operates at a temperature between 100.degree. F. above the temperature of a catalysthydrocarbon mixture exiting a riser and 1500.degree. F. The regenerator inlet temperature is controlled to obtain the desired regeneration temperature, regenerator outlet temperature, and degree of regeneration. The regenerator is maintained at a temperature between 100.degree. F. above that of the catalyst in the high temperature stripper and 1600.degree. F. The present invention has the advantage that it separates hydrogen from catalyst to eliminate hydrothermal degradation, and separates sulfur from catalyst as hydrogen sulfide and mercaptans which are easy to scrub.