Patent GB-743507-A (GB)
Title: Improved fluidised hydroforming process
IPC: B01J8/32
Filed: 1953-06-24
Abstract: <PICT:0743507/IV(a)/1> In a continuous process of hydroforming naphtha by contacting with a dense fluidized catalyst in a reaction zone, withdrawing catalyst, exothermically regenerating it in a regeneration zone, and returning it to the reaction zone, a different, finely-divided, inert material of larger particle size than the catalyst is passed into the regeneration zone, a mixture of said material and regenerated catalyst is withdrawn to a heating zone where it is mixed with catalyst taken from the hydroforming zone thereby heating the latter, catalyst is separated from said material and is returned to the hydroforming zone, and the said material is returned to the regeneration zone.  The heat transfer material may be copper, iron, stainless steel, mullite, alumina or titania.  It may have a particle size of 200-1000, preferably 400-600 microns, that of the catalyst being 20-300, preferably 40-150 microns.  The catalyst may be a metal oxide, e.g. Mo, Cr or V oxide, or Pt or Pd on alumina, with or without silica, which may be treated with halogen or halide. The weight ratio of heat carrier material to catalyst in the regenerator may be 1-8, preferably 3-5 : 1.  Residence time in the regenerator is 2-40, preferably 5-15 minutes.  Temperatures are 825-1050 DEG  F. in the reactor, 900-1200 in the regenerator, and 1000-1200 in the heater.  Pressure is 10-500 p.s.i.g.  In the heater, weight ratios of regenerated catalyst to catalyst from reactor, and of heat carrier material to catalyst from reactor of 1-6 : 1 are maintained.  Preheated naphtha is fed by line 2 and recycle gas by line 3 to the reactor 1 containing fluidized catalyst C.  This flows via stripping zone 7 and lines 9, 10, through which an air stream is passed, to regenerator 5 where it is mixed with heat transfer material, the mixture being suspended as a fluidized bed. The mixture after regeneration is charged to a pretreater 13, where it is conditioned by a stream of recycle gas, and thence to heater 17 where it mixes with catalyst from reactor 1 and standpipe 18.  Recycle gas from line 20 causes separation of catalyst, which is returned to the reactor by line 22, from heat transfer material, which is withdrawn through standpipe 23 and fed back to the regenerator in a stream of air through pipe 24.ALSO:<PICT:0743507/III/1> In a continuous process of hydroforming naphtha by contacting with a dense fluidized catalyst in a reaction zone, withdrawing catalyst, exothermically regenerating it in a regeneration zone, and returning it to the reaction zone, a different, finely-divided, inert material of larger particle size than the catalyst is passed into the regeneration zone, a mixture of said material and regenerated catalyst is withdrawn to a heating zone where it is mixed with catalyst taken from the hydroforming zone thereby heating the latter, catalyst is separated from said material and is returned to the hydroforming zone, and the said material is returned to the regeneration zone.  The heat transfer material may be copper, iron, stainless steel, mullite, alumina or titania.  It may have a particle size of 200-1000, preferably 400-600 microns, that of the catalyst being 20-300, preferably 40-150 microns.  The catalyst may be a metal oxide, e.g. Mo, Cr or V oxide, or Pt or Pd on alumina with or without silica, which may be treated with halogen or halide. The weight ratio of heat carrier material to catalyst in the regenerator may be 1-8, preferably 3-5:1.  Residence time in the regenerator is 2-40, preferably 5-15 mins.  Temperatures are 825-1050 DEG F. in the reaction, 900-1200 DEG  in the regenerator, and 1000-1200 DEG  in the heater.  Pressure is 10-500 p.s.i.g.  In the heater, weight ratios of regenerated catalyst to catalyst from reactor, and of heat carrier material to catalyst from reactor of 1-6:1 are maintained.  Preheated naphtha is fed by line 2 and recycle gas by line 3 to the reactor 1 containing fluidized catalyst C.  This flows via stripping zone 7 and lines 9, 10, through which an air stream is passed, to regenerator 5 where it is mixed with heat transfer material, the mixture being suspended as a fluidized bed. The mixture after regeneration is charged to a pretreater 13, where it is conditioned by a stream of recycle gas, and thence to heater 17 where it mixes with catalyst from reactor 1 and standpipe 18. Recycle gas from line 20 causes separation of catalyst, which is returned to the reactor by line 22, from heat transfer material, which is withdrawn through standpipe 23 and fed back to the regenerator in a stream of air through pipe 24.