Patent GB-780263-A (GB)
Title: Process for the destructive hydrogenation of hydrocarbon mixtures containing difficultly vaporizable components
Inventor: ANHORN VICTOR JOHN
IPC: C10G47/30
Filed: 1954-07-30
Abstract: Destructive hydrogenation of hydrocarbon mixtures which contain components which cannot be readily vaporized without substantial decomposition is effected in the presence of fluidized particles of hydrogenation catalyst composited with a porous carrier, at a tempera <PICT:0780263/III/1> ture of 750 DEG  to 950 DEG  F. and at a pressure between 250 and 2000 p.s.i.g., the rate of feed of liquid hydrocarbon components to the reactor being such that at least a proportion of the difficulty vaporizable components is maintained in the liquid phase on the catalyst particles.  Crude petroleum, reduced crude, topped crude, shale oil, heavy residual oils, and low-grade oils which contain large amounts of asphalt or sulphur may be treated by the process. An example relates to the destructive hydrogenation of Kuwait crude petroleum having a specific gravity of 0.87; this oil contained more than 50 per cent of components which do not distil at 590 DEG  F., and it contained 2.5 per cent sulphur.  A catalyst consisting of 1.5 per cent nickel oxide and 4.7 per cent tungsten oxide deposited on microspheroids (substantially 20-80 microns) of a synthetic silica-alumina base was charged to a reactor.  The catalyst was reduced by passing hydrogen through the reactor at atmospheric pressure and 900 DEG  F. for 2 hours.  After cooling to 800 DEG  F., the reactor was pressured with hydrogen to 500 p.s.i.g. The crude oil, and hydrogen (16.3 weight per cent of the oil were heated to 800 DEG  F. in a preheating coil and charged to the reactor which was maintained at 800 DEG  F. the percentage by weight of the charge remaining in the liquid phase being 10 per cent.  During the on-stream period, which lasted 4 hours, 3.5 weights of oil per unit weight of the catalyst were charged to the reactor at a space velocity of 0.87wt. oil/hr./wt. cat.  The product had a specific gravity of 0.795, and 83 per cent distilled over below 590 DEG  F.; the sulphur content was 0.2 per cent.  The reactor was purged with hydrogen for 3 hours, the temperature and pressure being the same as during the on-stream period.  The reactor was then depressured, purged with atmospheric nitrogen, and regenerated with preheated air for 5 hours.  A maximum temperature of 1023 DEG  F. was reached during the first hour of the regeneration.  The regenerated catalyst was cooled to 800 DEG  F., and the reactor was put on-stream again. The apparatus shown comprises two reactors 1 and 2 containing powdered catalyst which, by adjustment of the various valves, are alternately on-stream and undergoing regeneration.  The feed oil mixed with hydrogen is pumped through conduit 16 into heater 18, and thence via conduit 22 into reactor 1, or via conduits 24 and 28 into reactor 2.  Preheating in heater 18 is carried out so as to vaporize all the components which vaporize without decomposition, and leave the other components in the liquid phase.  The mixture is introduced into the lower portion of the catalyst bed in the reactor at such a rate as to maintain the catalyst particles in a suspended and turbulent state.  A linear velocity of the vapour in the range of 0.01 to 0.5 ft/sec. is suitable in this respect.  The product vapours pass out of the reactor through a cyclone, and then flow through conduit 54 into a recovery system (not shown).  When the catalyst in the reactor has accumulated sufficient carbon to reduce its activity, the mixture of oil and hydrogen is shunted to the other reactor; and the deactivated catalyst in the first reactor is regenerated in the fluidized state.  Purging hydrogen is pumped through conduit 30 to heater 18, and thence via conduit 22 or 28 into the base of the reactor containing deactivated catalyst. This hot hydrogen not only purges the hydrocarbons out of the reactor, but hydrogenates part of the carbonaceous deposit on the catalyst to give volatile hydrocarbons.  Steam or other inert gas is then introduced into the reactor via conduit 39.  After this, the regenerating gas (e.g. a mixture of air and steam) is introduced into the reactor via conduit 36.  The flue gas leaves the system via conduit 60 or 64.  After regeneration, the catalyst is cooled down with inert gas; and is then ready to go on-stream again.