Patent GB-732512-A (GB)
Title: Improvements in refining the products of a catalytic hydrocarbon conversion process
IPC: C10G11/18
Filed: 1951-11-22
Abstract: A process for refining the products of a hydroforming process comprises cooling the hot gasiform mixture of reaction products and entrained solid fines of catalytic material sufficiently to condense a major portion of the high-boiling normally liquid products, scrubbing the solid fines out of the uncondensed gasiform products by contact with the high-boiling condensate to form a slurry, settling the slurry, decanting a substantially solids-free portion of the high-boiling condensate from the settled slurry, removing relatively low molecular weight compounds from the decanted high boiling condensate by reducing the pressure thereon and <PICT:0732512/IV (b)/1> by contact with a gasiform stripping agent, and recovering the relatively low molecular weight compounds by separating them from the stripping agent.  In a fluidized process for hydroforming naphtha using a catalyst consisting of molybdenum trioxide and silica on an alumina gel support, the product containing entrained catalyst fines passes from the reactor 18 through lines 26, 114 to scrubber-fractionator 116 in the mid-section 116B of which a fraction (b.p. 400-700 DEG  F. and A.P.I. gravity 5-25 DEG ) condenses and scrubs catalyst fines from the remaining products.  From the bottom of the fractionating section 116A an oil is withdrawn at 122, used as a lubricant and flushing oil (e.g. in pumps 136, 138) and returned to the scrubber-fractionator.  A portion of the catalyst slurry is removed through line 142 by means of pumps 136, 138 and is cooled and returned to the top of the scrubbing section; the remainder of the slurry descends to settling section 116C from which a thickened slurry is pumped through line 156 back to the reactor, and catalyst-free oil is passed through line 162 to flash tower 164.  The overhead fraction from the fractionating section 116A is cooled and led to separating drum 170 where water and liquid hydrocarbons are removed; part of the liquid hydrocarbon is returned to the scrubber-fractionator through line 176 and part is led through line 174 into the middle of stabilizer 184, from which stabilized gasoline is removed at 190.  Part of the gas from the separating drum 170 is recycled back to the reactor through line 212, after being heated in heat exchangers 166, 112, and furnace 10, part passes through reducing valve 228 into absorber 4 where it contacts the naphtha feed, and the remainder is used, with or without steam, for stripping in flash tower 164.  A high boiling fraction (A.P.I. gravity 12 DEG ) is recovered from tower 164 through line 236, and the vapours leaving the tower 164 pass through line 240 to the absorber 4.  The naphtha feed passes from the absorber through furnace 10 and mixes with recycle gas before entering the reactor.ALSO:A process for refining the products of a catalytic hydrocarbon conversion process comprises cooling the hot gasiform mixture of reaction products and entrained solid fines of catalytic material sufficiently to condense <PICT:0732512/III/1> a major portion of the high-boiling normally liquid products, scrubbing the solid fines out of the uncondensed gasiform products by contact with the high-boiling condensate to form a slurry, settling the slurry, decanting a substantially solids-free portion of the high-boiling condensate from the settled slurry, removing relatively low molecular weight compounds from the decanted high-boiling condensate by reducing the pressure thereon and by contact with a gasiform stripping agent, and recovering the relatively low molecular weight compounds by separating them from the stripping agent.  In a fluidized process for hydroforming naphtha using a catalyst consisting of molybdenum trioxide and silica on an alumina gel support, the product containing entrained catalyst fines passes from the reactor 18 through lines 26, 114 to scrubber-fractionator 116 in the mid-section 116B of which a fraction (b.p. 400-700 DEG  F. and A.P.I. gravity 5-25 DEG ) condenses and scrubs catalyst fines from the remaining products.  From the bottom of the fractionating section 116A an oil is withdrawn at 122, used as a lubricant and flushing oil (e.g. in pumps 136, 138), and returned to the scrubber-fractionator.  A portion of the catalyst slurry is removed through line 142 by means of pumps 136, 138, and is cooled and returned to the top of the scrubbing section; the remainder of the slurry descends to settling section 116C from which a thickened slurry is pumped through line 156 back to the reactor, and catalyst-free oil is passed through line 162 to flash tower 164.  The overhead fraction from the fractionating section 116A is cooled and led to separating drum 170 where water and liquid hydrocarbons are removed; part of the liquid hydrocarbons is returned to the scrubber-fractionator through line 176 and part is led through line 174 into the middle of stabilizer 184, from which stabilized gasoline is removed at 190.  Part of the gas from the separating drum 170 is recycled back to the reactor through line 212, after being heated in heat exchangers 166, 112, and furnace 10, part passes through reducing valve 228 into absorber 4 where it contacts the naphtha feed, and the remainder is used, with or without steam, for stripping in flash tower 164.  A high boiling fraction (A.P.I. gravity 12 DEG ) is recovered from tower 164 through line 236, and the vapours leaving the tower 164 pass through line 240 to the absorber 4.  The naphtha feed passes from the absorber through furnace 10 and mixes with recycle gas before entering the reactor.