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    • 5. 发明专利
      GB994953A Continuous production of petroleum cokes 未知
    • Continuous production of petroleum cokes
    • GB994953A
    • 1965-06-10
    • GB3091963
    • 1963-08-06
    • MARATHON OIL CO
    • C10B55/02 , C10B55/06
    • A continuous process for making petroleum cokes comprises contacting coke particles with a fluid petroleum residuum to form a combustion charge and concurrently passing the charge and a combustion-supporting gas into a combustion zone 24 under conditions such that the zone remains stationary and only a minor portion of the charge, e.g. 2% to 15% by weight, is burnt, the remaining residuum being coked by heat from the zone. As shown, coke particles are fed downwardly into a retort 12 and may be preheated by gases delivered to the retort at 17, 18, the residuum, which may be liquid but is preferably vaporized, being delivered to the retort at 20, 21, in amounts of 8% to 25%, preferably 12% to 20%, by weight of the coke. The combustion supporting gas, which may be preheated, is delivered at 22, 23, and may be fluorine, chlorine, or nitrogen dioxide, but is preferably oxygen alone or with an inert gas, e.g. air or an oxygen-superheated steam mixture. Product coke is led off at 16, smaller coke recycled via lift 17a, and volatiles &c. led off at 27, non-condensibles, e.g. CO, C3H8, being separated at 28 for recycling, if desired, to the retort. Temperatures of 400 DEG to 1200 DEG C., preferably 750 DEG to 1200 DEG C., are maintained in the zone 24 by regulating preheat temperatures and coke and gas throughput, and the zone is held stationary by making the pressure in the top of the retort higher than in the zone 24. It is stated that the coke particles and the residuum may be fed to the retort in the form of a slurry.
    • 基本信息 添加关注 加入工作空间 PDF全文 PDF下载 全文下载 相似专利 双屏查看 权利要求书 说明书全文 Espacenet 法律信息 同族专利 专利引用
    • 7. 发明专利
      GB702909A Improvements in or relating to the cracking of hydrocarbons 未知
    • Improvements in or relating to the cracking of hydrocarbons
    • GB702909A
    • 1954-01-27
    • GB2458950
    • 1950-10-09
    • LUMMUS CO
    • SCHUTTE AUGUST HENRY
    • B01J8/12 , C10B55/06
    • Hydrocarbons are cracked to give inter alia substantial yields of C2 and C3 unsaturated hydrocarbons by passing a residual hydrocarbon feed into the upper part of a lower temperature bed of heated solid particles passing down by gravity alone in a reactor, maintaining a temperature of from 900 to 1100 DEG F. in the bed to mildly crack the liquid charge, passing vapours from the bed upwardly through a higher temperature bed of heated solid particles maintained at from 1100 to 1800 DEG F. to crack the vapours, quenching the cracked vapours and removing the quenched vapours at a position in the higher temperature bed corresponding to the desired cracking time. As shown heated solid particles, preferably non-catalytic, e.g. spent catalyst, petroleum coke, pumice, are fed into the top of a reactor 10 divided into two zones by a partition 24 provided with downpipes 28. The partition causes two beds to form, one below and one above the partition. Particles with an accretion of coke are withdrawn at 12, reheated to the required inlet temperature and recirculated. The liquid feed is introduced by line 20 and distributers 22 into the top part of the lower bed. Vapours formed flow upwards through the downpipes 28 into the higher temperature upper bed where they are cracked, the cracked vapours being withdrawn at the desired level through line 38 or line 40 connected to collecting channels 36 inside the upper bed. Inside each channel 36 is a distributor for quenching steam introduced through line 48 or 50. The vapour products may be separated into constituents and unwanted products (including gaseous olefines and light distillate) recycled with the feed. The vapour cracking time may be varied from several seconds to a fraction of a second by varying the speed of movement and temperature of the solids, and the depth of bed through which the vapours travel. Reheating of the particles may be accomplished by combustion of a portion of the coke formed on the particles. Vapours may be removed, if necessary, from the lower bed by pipe 30. Inlets 16 and 17 are provided for sealing steam and additional inlets may be provided for controlling the oil partial pressure in the two zones. An example is given of the cracking of a heavy residual oil of specified characteristics to give inter alia a C2-C3 gas stream containing 35 per cent. by volume of ethylene. Specification 653,740 is referred to.
    • 基本信息 添加关注 加入工作空间 PDF全文 PDF下载 全文下载 相似专利 双屏查看 权利要求书 说明书全文 Espacenet 法律信息 同族专利 专利引用
    • 8. 发明专利
      GB685056A Improvements in or relating to a reactor for and method of converting heavy liquid hydrocarbons into vaporous products and coke 未知
    • Improvements in or relating to a reactor for and method of converting heavy liquid hydrocarbons into vaporous products and coke
    • GB685056A
    • 1952-12-31
    • GB2306049
    • 1949-09-06
    • LUMMUS CO
    • C10B55/06
    • Heavy liquid hydrocarbons such as bottoms are cracked to produce volatiles and a coke residue by feeding preheated particle form contact material in one or more streams into the top of a reactor chamber, the streams forming flowing piles on the top surface of a gravity-packed bed of the particles moving down under gravity in the reactor, and feeding the liquid hydrocarbons into the streams of contact material or into the top portion of the flowing piles. The vapours which first flash off and those resulting from cracking during the downward passage of the oil in the bed are drawn off for further treatment and dry particles with a coke deposit are withdrawn at the bottom of the reactor and recirculated until grown to desired size. The bed particles may be, e.g. petroleum coke, pumice, spent cracking catalyst or crushed fire-brick. In the apparatus of Fig. 1 the insulated reactor 1 has a baffle plate 6 across its upper part from which depend nozzles 7, e.g. of circular or elongated cross-section, through which bed particles from a hopper and preheater 22 flow into the reactor. The particles build up into continuously moving cones or ridges at the top of the downwardly moving bed and pipes 8 are buried in these piles near their apices, the pipes having holes through which the oil flows outwardly and downwardly into the piles. The pipes are supplied from a manifold fed from line 10 and heater 9 and the whole pipe assembly can be removed as a unit for cleaning. Gases collecting in the free space beneath the baffle 6 are drawn off at 32. Purge steam is admitted at 30 and 31. The bottom of the reactor has flow control plates 11 and the outflow is regulated by a valve 14. Make-up material may be introduced at 15. The particles from the reactor are raised by elevator 13 and discharged into a grader 17 from which fines are discharged at 19, large particles (coke product) to line 20 and the remainder to preheater 22. Part of the coke product may be crushed at 21 and returned to the cycle at 15 if desired. The remainder may be partly calcined at 33 to remove remaining volatile material, the products of combustion being utilized to assist in the heating of the preheater 22. Further heat is supplied by burners 23 supplied with fuel gas and air from lines 25 and 26. Products of combustion are withdrawn at 28. In a modification oil feed pipes are located on either side of elongated nozzles 7 at their lower ends and direct oil into the sides of the flowing piles of particles. Alternatively the baffle may have rows of circular nozzles with oil pipes disposed between the rows to project oil into the sides of the resulting conical piles. In a pilot-scale plant, Fig. 7, oil is injected into the upper part of a conical pile of particles forming in the reactor 44 below a vertical feed pipe 46 from an annular feed passage 53 surrounding the lower end of the pipe. Flashed and cracked vapours are taken off at 50. In the arrangement of Fig. 11 oil is introduced through pipe 62 into the centre of a flowing column of particles fed into an outer concentric tube 60 from the elevator 13, the particles and oil being mixed by flowing over a series of baffles 64-67 increasing in size downward, the last baffle directing the particles into an annular flowing pile 68.
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