Uop Lcc

Jop Inc.

Harold U Hammershaimb

David A Lomas

Terry L Marker

Paul T Barger

Bipin Virpal Vora

Joseph A Kocal

Laurence O Stine

Gregory A Funk

Anthony G Vickers

Charles L Hemler

Tamotsu Imai

Robert R Frame

Daniel N Myers

Carlos A Cabrera

James F Himes

Joel B Spinner

Robert M Smith

Robert J Cornish

This process for the production of heavy oligomers by a combination of dehydrogenation and oligomerization uses a bed of saturation catalyst in a debutanizer to simplify the saturation and recycle of C.sub.4 hydrocarbons to the dehydrogenation zone. The catalytic distillation zone is located in the top of the debutanizer column and may offer further efficiency improvements to the process when used in series with a bed of alkylation or oligomerization catalyst in the distillation zone. The bed of alkylation or oligomerization catalyst reduces the quantity of C.sub.4 hydrocarbons recycled to the dehydrogenation zone by oligomerizing unconverted C.sub.4 olefins in the distillation column. Conversion of C.sub.4 olefins in the distillation column facilitates the operation of the oligomerization zone at lower conversion conditions that favor production of high octane products. The catalytic distillation arrangement is particularly beneficial in a combination for motor fuel from isoparaffins by dehydrogenation, oligomerization and saturation where the mass flow through the saturation zone is also reduced by alkylation and saturation in the distillation column.

Oligomer production with catalytic distillation

A process for the production motor fuel components from isoparaffins by dehydrogenation, oligomerization and saturation uses a combination of low severity dehydrogenation, first and second feed input locations and a primary separation column that receives feed and effluent components to deliver a dehydrogenation zone feed and a motor fuel products. A separation column receives the an isobutane input stream and a product containing effluent stream to distill a dehydrogenation zone input steam. The dehydrogenation zone operates at low severity conditions to produce the effluent stream that compliments the operation of an oligomerization zone by delivering an effluent stream that is higher in pressure and contains inert paraffinic diluent materials. The oligomerization effluent passes to a saturation reaction zone that provides a saturated effluent stream. The saturation zone effluent is divided to provide quench to both the oligomerization reaction zone and the saturation zone and saturated motor fuel components to the separation column.

Process for integrated oligomer production and saturation

An HF-agent complex, such as HF-pyridine complex where the complexing agent is pyridine, is recovered and recycled from a by-product containing stream in an alkylation process using the complex by (a) selectively removing a portion of the HF from the by-product stream to produce an HF-depleted stream having a molar ratio of HF per Lewis base site of the complexing agent of 3:1 to 5:1, (b) separating the resulting HF-depleted stream into a hydrocarbon phase enriched in ASO and an acid phase depleted in ASO and containing a substantial portion of the complex, and (c) recycling the acid phase to the hydrocarbon alkylation step.

Recovery and recycle of HF-amine complex in HF alkylation

A process for the efficient production of diisopropyl ether where catalytic distillation is used to increase the yield of product beyond thermodynamic equilibrium limitations has been developed. In a hydration zone the propylene in a feedstock is reacted with water in the presence of a catalyst to effect hydration to produce an effluent stream containing at least water, unreacted propylene, and isopropyl alcohol, and then, in an etherification zone, at least a portion of the effluent stream is further reacted by catalytic distillation in the presence of a catalyst to effect reaction of propylene and isopropyl alcohol to form diisopropyl ether while concurrently separating an organic portion containing the diisopropyl ether and an aqueous portion, and collecting the organic portion containing the diisopropyl ether.

Two-stage process for producing diisopropyl ether using catalytic

A process for the efficient production of diisopropyl ether where catalytic distillation is used to increase the yield of product beyond thermodynamic equilibrium limitations has been developed. In a hydration zone the propylene in a feedstock is reacted with water in the presence of a catalyst to effect hydration to produce an effluent stream containing at least water, unreacted propylene, and isopropyl alcohol, and then, in an etherification zone, at least a portion of the effluent stream is further reacted by catalytic distillation in the presence of a catalyst to effect reaction of propylene and isopropyl alcohol to form diisopropyl ether while concurrently separating a propylene rich portion, a diisopropyl ether rich portion and an aqueous portion, and recovering the diisopropyl ether from the diisopropyl ether rich portion.

Paraffins and other hydrocarbons are alkylated using a solid bed catalyst in a process featuring a reaction zone operated at mixed-phase conditions which allow the heat of reaction to vaporize a portion of the liquid phase feed hydrocarbon passing downward through it thus facilitating recycling of the feed hydrocarbon. The feed hydrocarbon recovered from the reaction zone effluent is recycled as a liquid, preferably admixed with hydrogen, with the feed olefin being preferably introduced near the top of the reactor as a vapor. The catalyst preferably contains a metal hydrogenation function effective to selectively hydrogenate C.sub.6 -plus olefins produced as by-products.

Mixed-phase solid bed hydrocarbon alkylation process

This invention provides a method of reducing the sulfur oxide emissions from the regenerator of an FCC process that cracks a sulfur containing feedstream. The sulfur oxide emissions are reduced by using an essentially sulfur free lift gas stream to shift the sulfur concentration equilibrium between the product stream from the reaction zone and the flue gas stream from the regeneration zone. Sulfur compounds present in the FCC feed leave the reaction zone as volatile sulfurous gases in the product vapor stream or as adsorbed sulfur compounds on the catalyst. Sulfurous gas in the product vapors is mainly H.sub.2 S. By lowering the concentration of H.sub.2 S that enters the riser with the lift gas the equilibrium reaction of sulfur with hydrogen in the riser is favorably shifted to increase the production of H.sub.2 S and decrease the lay down of sulfur compounds in the coke that forms on the catalyst. As a result less sulfur enters the regeneration zone with the spent catalyst and fewer sulfur oxides are formed during regeneration.

FCC process for reducing sox using H.sub.2 S free lift gas

Catalyst particles which are employed in reactions involving the conversion of organic compounds should possess a desired configuration in order to maintain a desired voidage which will permit passage of the feedstock through the catalyst bed during the conversion reaction. Solid phosphoric acid catalysts which comprise an admixture of an acid of phosphorus and a solid binder such as a siliceous material may be formed into polylobular, tubular, ridged, fluted, or channeled cylindrical particles which will permit a sufficient amount of voidage in the catalyst bed to be maintained even though the catalyst particles will swell during the reaction due to the formation of coke on the surface thereof.

Shaped catalyst particles utilizable for the conversion of organic

FCC catalyst is regenerated in a process providing increased coke-burning capacity without additional heat evolution or air consumption. The process uses a two-stage regeneration arrangement providing initial coke combustion in a low catalyst density-high efficiency contact zone followed by substantial separation of catalyst and regeneration gas and complete regeneration of catalyst particles in a dense bed regeneration zone. Catalyst and gas flow cocurrent prior to this separation but flow countercurrent after the separation. An effective control scheme for regulating oxygen addition to the final zone is also disclosed. This process is applicable to FCC operations for conventional and residual feedstocks.

Partial CO combustion with staged regeneration of catalyst

Olefinic feedstocks which contain catalyst contaminants or poisons such as sulfur containing compounds may be oligomerized to a desired product by effecting the reaction in the presence of an added amount of hydrogen to the feedstock. The catalyst which is employed to effect this oligomerization will remain stable and will not deactivate due to the presence of the aforementioned poisons. The catalyst composite will comprise a porous support which has been impregnated with a catalytically effective amount of an iron group metal compound and, if so desired, a compound containing a metal of the Group IVA of the Periodic Table. In addition, the catalyst composite will also contain in combination therewith, a catalytically effective amount of an alkyl aluminum compound and, if so desired, an aluminum alkoxy or aluminum halide compound.

Process for the oligomerization of olefinic hydrocarbons

A process using selective hydrogenation and HF alkylation in combination that employs a multifunction alkylation stripper for removal of light ends from the selective hydrogenation and a alkylation operations. The process combines the effluent from the selective hydrogenation operation, an isobutane feed stream and a bottoms stream from the HF stripper in the alkylation feed stripper. The feed stripper provides a C.sub.4 -plus bottoms stream that serves as the feed to the alkylation zone and a C.sub.3 -minus overhead that can be recovered as fuel gas. Significant benefit is obtained from this process when processing a mixed olefin feed of C.sub.3 /C.sub.4 hydrocarbons and recovering a high purity C.sub.3 product stream ahead of the selective hydrogenation zone. Another variation of this process allows a C.sub.3 product stream to be withdrawn from the alkylation feed stripper either directly as a sidecut or downstream of an overhead condensor.

HF alkylation and selective hydrogenation process

A process for converting a charge stock comprising normally liquid hydrocarbons in a riser conversion zone with an active fluid catalytic cracking catalyst wherein a suspension of hot regenerated active fluid catalytic cracking catalyst in a lift gas comprising hydrocarbons including not more than 10 mole % C.sub.3 and heavier hydrocarbons (calculated on a water-free basis) is passed through a first treatment section of the riser conversion zone at conditions selected to treat the catalyst prior to any contact with the charge stock while simultaneously accelerating the catalyst to a velocity sufficient to provide turbulent dilute flow at the point of contact with the charge stock; thereafter a charge stock is introduced into the suspension of treated particles in the riser conversion zone downstream of the treatment section to form a mixture of catalyst, charge stock and lift gas having the catalyst relatively uniformly distributed therethrough. The charge stock is then reacted with the catalyst in the remaining downstream section of said riser conversion zone at reaction conditions sufficient to effect the desired conversion.

Catalyst treatment and flow conditioning in an FCC reactor riser

A process for converting normally liquid hydrocarbons with an active fluid catalytic cracking catalyst which comprises:

Use of lift gas in an FCC reactor riser

A catalyst regeneration process and apparatus for the oxidative removal of coke from a coke contaminated fluid catalyst. The process comprises a high temperature coke combustion zone, a catalyst disengagement zone and an external heat removal zone. A mixture of coke contaminated catalyst, oxygen containing gas, hot regenerated catalyst and cool regenerated catalyst from the heat removal zone are contacted in the high temperature combustion zone, the temperature of which is controlled by adjusting the rate at which catalyst is recycled from the heat removal zone. The temperature of the catalyst-gas mixture is controlled by adjusting the rate at which hot catalyst is recycled from the disengagement zone.

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Western Springs, IL, United States of America

Harold U Hammershaimb