Texaco Inc.

Texaco Development Corporation

Glenn A Clausen

David E Self

Gerald V Nelson

Ajit K Bhattacharya

Govanon Nongbri

Charles H Schrader

Michael K Porter

Philip A Lane

Christopher A Paul

Kathryn P Weldon

Jeffery B Harrison

Karen A Kuhn

An improved ebullated bed hydroconversion process is disclosed that utilizes a bimodal heterogeneous catalyst and a metal containing oil-miscible-catalysts compound to achieve a reduction in sediment, an increase in conversion, a reduction in the energy utilized to maintain reaction conditions and increases the stability of the ebullated catalyst bed. The oil-miscible compound may be provided in a concentration so as to provide about 1 to about 60 wppm metal based on the charge hydrocarbon oil.

Hydroconversion process

Hydroconversion of heavy hydrocarbon oils using solid heterogeneous catalyst and small amounts of oil-miscible compound, like molybdenum naphthenate, improves total pore volume properties of the catalyst.

Hydroconversion process and catalyst

An improvement has been discovered in an ebullated bed process. A residual hydrocarbon oil feedstock is hydrocracked to yield a product oil. The amount of sediment in the product oil is controlled by adjusting hydrogen partial pressure according to an algorithm. A change in temperature and residence time is avoided.

Ebullated bed process

A feedstock comprising 10 to 15 wt % used motor oil is subjected to delayed coking to yield coke and distillate fractions.

Delayed coking of used lubricating oil

In an ebullated bed process, a nominal 1000.degree. F.+ boiling point vacuum residuum is hydrotreated at a first temperature of 750.degree. F. to 875.degree. F. and total pressure of 1900 psig to 3000 psig. Hydrogen partial pressure is controlled by changing total reactor pressure in the range of 1700 psig to 2300 psig to achieve a selected yield of 650.degree. F.- boiling material.

Controlling hydrogen partial pressure to yield 650 .degree. F.- boiling

In a ebullated bed process, a residual hydrocarbon oil is hydrotreated at a reaction temperature of 750.degree. F. to 875.degree. F. and pressure of 1500 psig to 10,000 psig in a single or multiple reaction zone. A sample of hydrotreated liquid effluent is flash separated to obtain a nominal 650.degree. F.+ liquid which is magnified to 100.times.. Area precent, average diameter and maximum size of insoluble agglomerates is measured from the magnified view. Reactor temperature is varied with the area percent, average diameter and maximum size of insoluble agglomerates to control downstream sediment formation and plug formation at an acceptable level.

Microscopic examination of ebullated bed process effluent to control

A mixture of hydrocarbons consisting of gas oil and residual oil is catalytically cracked in the presence of a fluidized zeolite catalyst. The mixture of hydrocarbons is classified by boiling range as a 550.degree.-1000.degree. F. gas oil and a 1000+.degree. F. vacuum residuum. The gas oil is selectively cracked using a freshly regenerated fluid zeolite catalyst having less than 0.1 wt % residual carbon to give a high yield of desirable liquid hydrocarbon boiling from about 60.degree.-670.degree. F. The vacuum residuum is injected into the riser reactor at a point near the riser outlet to quench the cracking reactions in the gas oil. The vacuum residuum undergoes a small amount of reaction removing undesirable materials and yielding a liquid hydrocarbon boiling up to about 1000.degree. F. The amount of vacuum residuum cracking and overall yield of liquid hydrocarbons are controlled by downstream injection of vacuum residuum into the riser.

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Nederland, TX, United States of America

Glenn A Clausen