Phillips Petroleum Company

Paul D Hann

Charles C Chapman

Thomas Hutson, Jr

Joe Van Pool

John R Casperson

Thomas J Gunnell

Donald J Makovec

Tom Hutson, Jr

Bernhard H Geissler

Robert A Carle

Joe VanPool

Donald M Little

A continuous process for alkylating an alkylatable hydrocarbon in the presence of a acid-type catalyst in which the alkylatable hydrocarbon is contacted with an alkylating agent in the presence of a catalyst in a reaction zone so as to alkylate the alkylatable hydrocarbon. The reaction product is separated in an acid settler vessel into an alkylate product phase, located in the upper portion of the first separation zone, and a catalyst phase located in the lower portion of the first separation zone. The catalyst phase is further separated into a first portion and second portion, such that the first portion is cooled and recycled for use in the alkylation reaction zone as a catalyst recycle, and the second portion is passed into a second separation zone, wherein the catalyst phase is further separated into a rerun catalyst stream containing acid-type catalyst and an acid soluble oil stream. The rerun catalyst stream is passed into the hydrocarbon phase of the acid settler vessel. In order to prevent excessive pressure in the acid settler vessel as a result of the hot rerun catalyst stream, two liquid hydrocarbon drawoffs from the acid settler vessel are employed. The warm upper drawoff of the acid settler vessel is charged as feed to a depropanizer and stripper and the cool lower drawoff of the acid settler vessel is charged as reflux feed to an isostripper. The acid settler vessel contains a pressure controller set to the desired pressure to be maintained in the upper portion of the acid settler vessel. As the pressure in the acid settler vessel increases, a valve connected to the cool lower drawoff is closed and a valve connected to a conduit attached to the warmer upper drawoff is further opened such that an increased amount of hot hydrocarbon is shifted to the isostripper so as to lower the heat in the acid settler vessel thereby maintaining the desired pressure in the acid settler vessel.

Catalytic alkylation apparatus

A continuous process for alkylating an alkylatable hydrocarbon in the presence of a acid-type catalyst. The reaction product is separated in a first separation zone into an alkylate product phase, located in the upper portion and a catalyst phase located in the lower portion. The catalyst phase is separated into a first portion and second portion, the first portion is cooled and recycled for use in the alkylation reaction zone, and the second portion is passed into a second separation zone, wherein the second portion catalyst phase is further separated into a hot rerun catalyst stream and an acid soluble oil stream. The rerun catalyst stream is passed into the alkylate product phase of the first separation zone. In order to prevent excessive pressure in the first separation zone as a result of the hot rerun catalyst stream, two liquid hydrocarbon drawoffs from the first separation zone are employed. The hotter upper drawoff of the first separation zone is charged as feed to a depropanizer and stripper zone and the cooler lower drawoff of the first separation zone is charged as reflux feed to an isostripper zone. The pressure in the upper portion of the first separation zone is determined. As the determined pressure increases, the flow rate of the cooler lower drawoff is decreased and the flow rate of the hotter upper drawoff is increased such that an increased amount of hot hydrocarbon is shifted to the isostripper zone so as to lower the heat in the first separation zone.

Catalytic alkylation process

In a combination alkylation-methyltertiary butyl ether (MTBE) operation, the unreacted C.sub.4 olefinic hydrocarbons produced by etherification are contacted with molecular sieves to absorb 2-butenes and the 1-butenes remaining in the stream are divided so that one portion is subjected to double bond isomerization to form 2-butenes for alkylation and another portion is subjected skeletal isomerization to form isobutene for etherification.

Hydrocarbon conversion process

In a combination alkylation-methyltertiary butyl ether (MTBE) operation, isobutane vapor side-draw and bottoms product yield from the alkylation fractionation, respectively, are used to indirectly heat the mid-section and reboil section of the methyltertiary butyl ether fractionator for heat conservation, beneficiating both the alkylation operation and the MTBE operation.

Combination alkylation-etherification process

A carbon black reactor employs the following components to produce non-uniform gas flow patterns.

Process for production of carbon black

MTBE is recovered from an ether containing effluent by fractionation. When driers are not used on the hydrocarbon feed to MTBE manufacture, a separate water-methanol phase occurs in the fractionation overhead which is separately processed in a methanol fractionator and the water recovered is used to water wash the separated hydrocarbon phase from the overhead while methanol is recycled to MTBE and when driers are used on the hydrocarbon feed a separate methanol phase occurs in the fractionation overhead which can be recycled to MTBE manufacture and the hydrocarbon phase is directly passed to a drier preceding alkylation.

Ether recovery

A method for removing organic fluorides from HF alkylation propane in which a stream of relatively pure liquid HF obtained by settling liquid HF from the liquefied hydrocarbon passed to the overhead accumulator common for both the depropanizing column and a hydrogen fluoride stripping column is intimately contacted with a stream of liquid hydrocarbon containing organic fluorides derived from condensing the mixed overhead vapor from a depropanizing column and overhead vapor from an HF stripping column in the process of separating products from a hydrogen fluoride alkylation. In preferred embodiments, the contacting takes place in the static mixer.

Removal of organic fluorides from HF alkylation products

In an HF alkylation process, ASO is separated from HF acid catalyst in a fractionation zone by heating the fractionation zone with a condensible stream comprising liquid and vaporous components. In the process of condensation, latent heat is evolved which is used to effectuate the separation of ASO and HF acid catalyst and dilution of the separated ASO is achieved with the use of the produced condensate.

HF Alkylation process

A carbon black reactor to produce non-uniform gas flow patterns utilizes

Carbon black reactor with angled combustion chamber and non-aligned

A process combination, with inter-cooperation, for producing high-octane alkylates comprising

Production of high-octane, unleaded motor fuel by alkylation of

A process for maintaining HF acid soluble oils (ASO) in an HF alkylation reaction zone in an amount sufficient to ensure formation of an alkylate containing a high octane number is provided by returning to the reaction zone a portion of acid soluble oil recovered from an HF catalyst rerun system.

Dialkyl ether is produced by passing isoolefin, alkanol and diluent through a series of catalyst zones, cooling the effluent between zones and adding isoolefin and/or alkanol between zones.

Dialkyl ether production

Propylene and butylenes are separately acid alkylated with at least one isoparaffin. Expansion and liquid-vapor separation is utilized to separate the propylene from the butylenes. The use of expansion and separation improves the energy efficiency of the alkylation process. The energy efficiency of the alkylation process is further improved by utilizing the bottoms product from the acid stripper associated with the isostripper to cool the acid being supplied to the riser reactor. The size requirements of the isostripper are also reduced by using liquid-vapor separation to remove at least a portion of the unreacted isoparaffin from the alkylated butylenes.

Alkylation process

A process is provided for the alkylation of isoparaffins with olefins in the presence of an HF acid catalyst comprising separating a liquid hydrocarbon phase from the alkylation effluent, subjecting the hydrocarbon phase to HF stripping, separating the stripped hydrocarbon into a liquid and a vapor phase, fractionating the liquid phase into product streams, and pressurizing the vaporous stream prior to separation of C.sub.3 and lighter materials. The HF alkylation process utilizes indirect heat exchange of various streams and compression of HF-free vapors.

Alkylation separation process

A process is provided for the simultaneous and separate alkylation of an isoparaffin such as isobutane with different olefins, e.g., propylenes and butylenes in different zones with an HF acid catalyst comprising separating the hydrocarbon phase from each of the alkylation effluents, subjecting each hydrocarbon phase to separate HF stripping, fractionating the liquid phases removed from each of the HF stripping zones, pressurizing the vaporous isoparaffin stream recovered from fractionation and utilizing the pressurized vaporous streams for indirect heat exchange with HF strippers and fractionation zones prior to recycling through alkylation.

Growing community of inventors

Bartlesville, OK, United States of America

Paul D Hann