Exxon Research and Engineering Company

Exxon Chemical Patents, Inc.

Exxonmobil Research and Engineering Company

Willibald Serrand

Mitchell Jacobson

John F Pagel

Michael R Parrish

David G Hammond

Paul K Ladwig

Martin C Poole

Hans A Weisenberger

Noel M Seimandi

Tony T Cheng

Paul E Eberly

Todd R Steffens

Udo Zentner

Patrick H Terry

Ingo Dreher

Robert C Green

Philip Holmes

Norman H Sweed

Hans J M Weiss

Jorg H Schmalfeld

Noel Seimandi

Norman Harris Sweed

An improved process for deasphalting a residua feedstock by use of a short vapor residence time process unit comprised of a horizontal moving bed of fluidized and/or stirred hot particles. The vapor phase product stream from said process unit is passed to a soaker drum where a high boiling fraction is separated and recycled to the process unit after undergoing reactions causing molecular weight growth. This reactive recycle using the soaker drum results in substantially improved qualities of the liquid products compared with what is achieved by once-through residua deasphalting process alternatives.

Process for deasphalting residua by reactive recycle of high boiling material

A two-stage process for converting petroleum residua and other low value oils to high valued gasoline blendstocks and light olefins. The first stage is comprised of a thermal process unit containing a reaction zone comprised of a horizontal moving bed of fluidized hot particles operated at temperatures from about 500 to 600&deg; C. and having a short vapor residence time, and the second stage is comprised of a catalytic conversion zone operated at a temperature of about 525&deg; C. to about 650&deg; C., and also having a short vapor residence time, preferably shorter than that of the first stage reaction zone.

Two-stage process for converting residua to gasoline blendstocks and light olefins

A process for obtaining a substantial amount of olefinic products from a residual feedstock by use of a vapor short contact time conversion process unit comprised of a bed of fluidized heat transfer solids. The vapor short contact time process unit is operated at conditions which includes steam dilution to reduce partial pressure of hydrocarbon vapors and a vapor residence time less than about 0.5 seconds.

Process for obtaining olefins from residual feedstocks

A process for producing normally gaseous olefins from two different process units sharing common downstream quench and fractionation facilities, wherein one of the process units is a short contact time mechanically fluidized vaporization unit for processing petroleum residual feedstocks and the other is a conventional steam cracking unit.

Dual process for obtaining olefins

A process wherein a residuum feedstock is upgraded in a short vapor contact time thermal process unit comprised of a horizontal moving bed of fluidized hot particles, then fed to a fluid catalytic cracking process unit. Hot flue gases from the fluid catalytic cracking unit is used to circulate solid particles and to provide process heat to the thermal process unit.

Integrated residua upgrading and fluid catalytic cracking

A two-stage process for obtaining a substantial amount of olefinic product from a residua feedstock. The first stage is comprised of a thermal process unit containing a reaction zone comprised of a horizontal moving bed of fluidized hot particles operated at temperatures from about 500.degree. to 600.degree. C. and having a short vapor residence time, and the second stage thermal conversion zone operated at a temperature of about 700.degree. C. to about 1100.degree. C., and also having a short vapor residence time.

Two-stage process for obtaining significant olefin yields from residua

A process for deasphalting a residua feedstock by use of a short vapor contact time thermal process unit comprised of a horizontal moving bed of fluidized hot particles. It is preferred that a mechanical means be used to fluidize a bed of hot particles.

Process for deasphalting residua (HEN9511)

A process for obtaining a substantial amount of olefinic products from a residua feedstock by use of a short vapor contact time thermal process unit comprised of a horizontal moving bed of fluidized hot particles.

Process for obtaining significant olefin yields from residua feedstocks

An improved fluidized bed coking process wherein a residuum feedstock is introduced into a first stage comprised of a short vapor contact time reactor containing a horizontal moving bed of fluidized hot particles. Carbonaceous material is deposited onto the hot particles on contact with the hot particles, and a vapor product is produced. The hot particles, containing the carbonaceous deposits, are fed to a second stage fluidized bed coking process.

Fluidized bed coking process

Process and apparatus for dehydrogenating alkanes

A catalytic cracking process and apparatus wherein particles of cracking catalyst circulate continuously between a reaction zone and a regeneration zone and hot regenerated catalyst from the regeneration zone contacts hydrocarbon feed in the reaction zone to produce cracked hydrocarbon products and spent catalyst. The spent catalyst is recovered and subjected to stripping in a stripping zone to remove strippable material therefrom. The stripped spent catalyst is circulated to the regeneration zone for oxidative exothermic regeneration. Some hot regenerated catalyst is passed directly from the regenerator to the stripping zone via a conduit provided for this purpose. Another hydrocarbon stream is passed into contact with the hot regenerated catalyst in this conduit. The said other hydrocarbon stream is converted to products of enhanced value (e.g., olefins) during contact with catalyst in the conduit, and the said products are recovered. The heat for the conversion is abstracted from the catalyst particles passing via the pipe to the stripping zone. The hot catalyst particles entering the stripping zone from the pipe increase the temperature in the stripping zone, thereby improving the stripping in the stripping zone.

Catalytic cracking process with circulation of hot, regenerated catalyst

Claus tail-gas containing H.sub.2 S and SO.sub.2 in a mol ratio of 2:1 is passed in contact with a catalyst-adsorbent bed (19A) at a temperature of 135.degree. to 150.degree. C. and a space velocity of 50 to 1500 h.sup.-1 whereby elemental sulfur produced by the reaction of H.sub.2 S and SO.sub.2 is deposited upon and/or adsorbed on said bed. The resulting sulfurous gas mixture is cooled by indirect heat exchange (26) to a temperature of 120.degree. to 135.degree. C. and liquid elemental sulfur is recovered (27,54,55,101) the sulfurous gas (28) thereafter being cooled and diluted by adding cool inert gas (34) thereto to maintain the water partial pressure below the saturation vapor pressure, and the cooled diluted gas mixture is contacted with a bed of catalyst-adsorbent (32A) at a temperature of 90.degree. to 125.degree. C. whereby further elemental sulfur is produced by the reaction of SO.sub.2 and H.sub.2 S. The elemental sulfur deposits upon and/or is adsorbed on the catalyst-adsorbent and the resulting purified gas (34) is incinerated (37) and discharged (38) to the atmosphere. In one embodiment, the gas from the indirect heat exchange step (26) is contacted with catalyst-adsorbent (30A) at 120.degree. to 135.degree. C. before cool inert gas (34) is mixed therewith, elemental sulfur being deposited upon and/or adsorbed on the catalyst-adsorbent. Elemental sulfur is removed from the catalyst-adsorbent beds by a hot, inert purge gas (44,46) which is cooled (19B,52) for sulfur recovery. The purge gas is cooled (52) at the end of the sulfur-recovery step to cool the catalyst-adsorbent beds for a further cycle of sulfur recovery from Claus tail-gas.

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Buxheim, Germany

Willibald Serrand