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公开(公告)号：GB759260A
公开(公告)日：1956-10-17
申请号：GB2909252
申请日：1952-11-18
Applicant: STANDARD OIL DEV CO
Inventor： LEWIS WARREN KENDALL
IPC: C22B1/10
Abstract: Sulphur dioxide free from elemental sulphur, oxygen and sulphur trioxide are obtained from a metal sulphide ore which liberates free elemental sulphur on heating, by fluidizing the finely divided ore with an oxidizing gas in a distillation zone, the temperature and quantity of the gas being such that a portion of the sulphur in the distillation zone is oxidized to sulphur dioxide thereby generating sufficient heat to distil all the distillable remaining sulphur from the ore as elemental sulphur, withdrawing the sulphur vapour and sulphur dioxide overhead from the distillation zone and passing the solids from the distillation zone as a suspension in a second gas containing free oxygen into a roasting zone where the ore is fluidized with an oxidizing gas having an amount of oxygen insufficient to oxidize all the sulphur present and withdrawing and collecting a gas containing sulphur dioxide free from trioxide, oxygen and sulphur from a space above the fluidized bed of the first roasting zone. Preferably the sulphur vapours obtained from the distillation zone are burnt in a sulphur burning zone to produce sulphur oxides which together with excess oxygen are in part employed as the second oxidizing gas. The solids withdrawn from the roasting zone may be passed to a second zone where, fluidized by a free oxygen containing gas, they are stripped of residual sulphur. As shown in the Figure, ironpyrites, for example, is fed from hopper 1 to a distillation vessel 3 where it is fluidized by an oxygen containing gas entering at 6 whereby the pyrites is converted to ferrous sulphide and the sulphur and sulphur oxides formed are withdrawn through pipe 19 to a sulphur burning zone 20 to which air or oxygen is supplied by lines 18 or 21. The solids are withdrawn from the distillation zone through a pipe 10 and passed to a first roasting zone 30 as a suspension in an oxidizing gas entering through line 15 and comprising the off gases from the sulphur burning chamber 20, the pipe 10 being of sufficient length so that any unchanged pyrites is allowed to react with ferrous oxide to produce ferrous sulphide and sulphur dioxide in the pipe 10. On passage to the first roasting zone 30 the solids are fluidized by an oxidizing gas entering from below and the product gases leave through a heat exchanger 36. The solids from the first roasting zone 30 are then passed through a conduit to a second roasting zone 38 supplied with air pre-heated in heat exchangers 36 and 26 (the latter recovering the heat from the sulphur burning step) through line 41 and with cold air through lines 44. The iron oxide freed from sulphur is withdrawn at 49 and the oxygen containing gases leaving the second roasting zone 38 are passed to the first roasting zone through line 45 or through valve 47 to the distillation zone through pipe 6, or to the sulphur burning zone through line 18. Air may be supplied to the system through lines 21, 13 and 43 and aerating jets may be provided in the pyrites feed line and in the draw-off from the distillation vessel 3. The temperature of the distillation zone, the pipe 10, the roasting zone 30 and the second roasting zone 38 are all maintained below the sintering temperature of the solids, preferably below 1800 DEG F. Specification 710,987 is referred to.
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公开(公告)号：DE950398C
公开(公告)日：1956-10-11
申请号：DEST006458
申请日：1953-05-24
Applicant: STANDARD OIL DEV CO
IPC: C10G35/14
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公开(公告)号：DE948375C
公开(公告)日：1956-08-30
申请号：DEST008643
申请日：1954-08-22
Applicant: STANDARD OIL DEV CO
IPC: C10L1/18
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Patent Agency Ranking
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公开(公告)号：FR1119834A
公开(公告)日：1956-06-26
申请号：FR1119834D
申请日：1955-01-18
Applicant: STANDARD OIL DEV CO
Abstract: Hydrocarbon oils such as gas oil are cracked by passing a suspension of hot catalyst particles in the hydrocarbon vapours upwards through a reactor 10 at a velocity of at least 6 feet per second and separating the cracked products from the spent catalyst. The carbonaceous deposit is burned off the spent catalyst by passing it with oxygen-containing gas through regenerator 40 at a velocity of at least 6 feet per second; a major proportion of the hot regenerated catalyst is recycled to the inlet of the regenerator, and the remainder is mixed with fresh hydrocarbon feed flowing to the reactor. Because the hydrocarbon vapours expand in volume as cracking proceeds, reactor 10 is made in the shape of a slender inverted cone. The catalyst may be synthetic silica-alumina, silica-magnesia boria-alumina or natural clay, and preferably has a particle size of 20 to 100 microns. Gas oil, preheated to about 675 DEG F., is introduced into the system through conduit 13, and is vaporized by hot regenerated catalyst (5 to 6 parts per part by weight of oil) flowing through conduit 11. The mixture of catalyst and hydrocarbon vapours then passes upwardly at a superficial velocity of about 10 ft./sec. through reactor 10 where the pressure is about 10-25 p.s.i.g., the temperature about 850 DEG -1000 DEG F., and the density of the mixture about 6 lbs./cubic foot. There is about 55 per cent conversion in the reactor. The mixture flows out through rough cut cyclone 15, which contains moving vanes, into separation chamber 16. The catalyst particles are thrown tangentially outwards into the lower portion of this chamber; and residual catalyst is separated from the hydrocarbon vapours by cyclone 18. The hydrocarbon vapours are introduced through conduit 22 into fractionating equipment (not shown) to separate gasoline and other products. The catalyst is withdrawn from chamber 16 through conduit 17, and flows to stripper 30 which contains baffles and is supplied with steam through conduit 31. The steam flows up through the downwardly-cascading catalyst, and strips entrained hydrocarbons therefrom. The steam and hydrocarbon vapours are introduced into chamber 16. The stripped spent catalyst flows down conduit 34, and is conveyed into the bottom of regenerator 40 by air introduced through conduit 35. Hot regenerated catalyst is introduced into the bottom of the regenerator through conduit 41. The ratio of recycle catalyst to spent catalyst is about 3 : 1. Auxiliary burner 42 at the base of the regenerator is normally used only during the starting-up of the plant, when the burner is supplied with fuel through line 43. Air is supplied to the burner through line 45, and the flow of air through this line is continued during on-stream operation. The mixture of catalyst and air flows upwards through the regenerator at a superficial velocity of about 10 ft./sec. The average temperature in the regenerator is 1000 DEG -1200 DEG F., the average pressure is 5 to 15 p.s.i.g. and the density of the catalyst/air mixture is about 8 lbs./cubic foot. The hot regenerated catalyst and flue gases pass through rough cut cyclone 48 into separation-chamber 47. The flue gases finally flow out through cyclone 50. The separated catalyst passes through conduit 49 into hopper 60. About threequarters of this hot regenerated catalyst is recycled to the regenerator through conduit 41, and the remainder flows through conduit 11 to reactor 10. The flow of catalyst through conduit 41 is controlled by the amount of aeration gas introduced therein through conduit 65, which is controlled by valve 66. In order to overcome loss of catalytic activity due to metallic deposition, part of the catalyst is withdrawn from the system through line 80, and is replaced by fresh catalyst introduced into conduit 65. Hopper 70 contains the fresh catalyst, and this is introduced into the cracking system through line 76 and conduit 78, fluidizing air being introduced through lines 73 and 79. About 12 per cent of the total catalyst in the system is replaced by fresh catalyst per day. Specifications 558,879 and 716,242 are referred to.
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