BE501713A - - Google Patents

Description

       

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  PROCESS AND APPARATUS FOR THE TRANSFORMATION OF HYDROCARBONS.



   The invention relates to methods for the conversion of fluid hydrocarbons in the presence of a granular contact substance, which may or may not be catalytic in nature. Typical processes to which the present invention applies are: catalytic cracking, isomerization, hydrogenation, "reforming", dehydrogenation, aromatization, "hydroforming", processing and desulfurization. of petroleum fractions. Other typical processes are: coking, reduction of the viscosity of oil residues and high temperature transformation processes by pyrolysis, such as the conversion of propane and ethane to ethylene or from methane to acetylene.

   In these latter methods, the granular contact substance serves only as a heat transfer material.



   The apparatus for the continuous conduct of reactions of this type, where, - the granular contact material is caused to pass in a cyclic manner through a hydrocarbon transformation zone or reaction zone and a substance regeneration zone Contact, apparatus in which this substance flows downward in the form of an essentially compact column, constitutes an important industrial installation.

   The contact substance employed in such a process may consist of a catalyst in the form of natural and treated clays, bauxites, inert vehicles impregnated with certain catalytically active metal oxides, or synthetic combinations of silica, alumina, magnesia, or combinations thereof, to which small amounts of metal oxides may be added for specific applications. When the contact substance is used only for the purpose of heat transport, it can be in the form of metal balls, capsules containing fusible alloys, pebbles, carborundum, mullite, zirconium oxide, molten alumina, and the like.

   For coking processes, the solid material may consist of a low activity clay catalyst, petroleum coke, or an inert porous material, such as pumice. The contact substance may be in the form of pellets, spheres, tablets or irregularly shaped particles, and it should be noted that the term "granular" is used herein in a broad sense and covers any of

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 forms above. The sizes of the granules of the contact substance range from about 12.7 mm to 80 mesh of the Tyler series and should preferably be in the range of 4 to 20 mesh.



   The invention relates to an improved system for carrying out reactions of the type described above, in the presence of a granular contact substance moving in a cyclic fashion; it relates particularly to the part of such a system in which a. the circulation of this contact substance takes place.



   Hitherto it was customary in industrial installations to arrange the reaction and regeneration chambers side by side and to circulate the contact substance between these chambers by means of bucket elevators. Such elevators do not give satisfaction in operations, which are carried out at extremely high temperatures, - in view of the 'mechanical' failures to which they are subject; moreover, in practice they impose unfavorable restrictions on the maximum flow rate of the contact substance in circulation.

   It has already been proposed to extract the contact substance from one of the contacting chambers by means of a throttled outlet tube from which this substance passes into a high-speed lifting gas jet. , and at high pressure, whereby is suspended and raised to the other contacting zone These systems have not been employed in industrial cracking installations using a granular contact substance, since their use in such processes gives rise to various serious difficulties. The lift gas employed in the proposed systems is supplied by a compressor and due to the very large pressure drop in the riser tube, these lift systems require a large expenditure of motive power.



  In addition, and since there is a large pressure at the lower end of the lift current, there is a serious problem in introducing the contact substance into the lift current. lift gas, especially when the contacting zone from which this substance passes into the lift stream is operating at a low pressure, that is, lower than the pressure of the lift stream. Another very serious disadvantage of such transfer systems is that the high speed gas jet which is generally introduced into the lower end of the lifting gas tube causes marked attrition of the contact substance. , which turns into fines, as well as erosion of the switchgear.

   Further, and while under certain conditions of linear flow velocity of gas and contact substance, significant attrition of this substance in the riser itself can be avoided, this result cannot be avoided. ensured in the lift gas processes known to date, since in these latter processes the possibility of making changes in the quantity of contact substance transferred per unit of time generally depends on a change in the overall flow rates of the gas. This means that a required change in the flow rate of the circulating contact substance may necessitate a change in the gas velocities in the lift gas stream,

   modifications which are not favorable from the point of view of attrition of the contact substance. Some earlier gas lift systems, using high speed ejectors, depended for the control of solids flow not only on a change in the velocity of the exhaust gas, but also on a change in the special relationships in. - Be the gas and solid material inlet openings; one relative to the other and relative to the lower end of the elevator gas tubes.

   As much of the attrition losses can occur in the area of the entry point of the high velocity jet, a slight change in the special rela- tionships which occur in this area in the gas lift systems of this last type can have a very detrimental effect on. attrition rates of the contact substance.



   One of the main objects of the present invention is to establish an improved method and apparatus for carrying out transformations of hydrocarbons in the presence of a moving granular contact substance.



   A specific object of the invention consists in providing, in such a method, a new and improved method and apparatus for ensuring

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   @ the circulation of the contact substance and to control the speed of this circulation.



   Another object of the invention is to provide an improved method and apparatus for the introduction of the contact substance into a rising gas stream, which will make it practically possible to circulate the contact substance. granular in continuous catalytic cracking systems, this by pneumatic transport means.



   The above stated objects, as well as other objects of the invention, will become apparent from the following discussion.



   According to an embodiment of the invention, the contact substance is directed downwards in a circuit comprising in series two contacting zones arranged one above the other, one of these, zones being that of transformation of hydrocarbons, while the other co-constitutes the zone of regeneration of the contact substance. The latter runs downward by gravity from the lower contacting zone and in the form of a compact stream flowing into a compact bed of contact substance contained in a feed zone of the elevator system. . An elevation tube extends upwardly from the interior of this bed and to a separation zone located above the upper contacting zone.



  The lower end facing downwards, of the riser tube, is in open communication, over at least part of its passage section, with said lito A first stream of riser gas is directed upwards to terminate at the lower end of the riser tube and without having to pass through a substantial thickness of the bed of contact substance. An elevating gas feed stream is passed through a substantial thickness of this bed and then entering the lower end of the riser tube so as to force or cause the contact substance forming part of the bed. this bed to flow to the first upward flow of lift gas.



  The rate at which the contact substance enters the riser tube is controlled by adjusting the amount of the feed gas stream. The lift gas stream can enter the lift tube at a pressure suitable to effect the desired transport of contact substance; however, in the preferred variations of the invention, the lifting gas and the contact substance which have entered the lower end of the lifting tube are sucked up from the bottom up by the effect of the vacuum maintained in the receiving area or separation. The separated lift gas is evacuated from the separation zone, so as to maintain the vacuum therein.

   The contact substance is separated from the lift gas in the separation zone and travels downwards, to the upper contacting or processing zone, through an unobstructed gravity feed duct of sufficient height. to overcome the pressure difference between these two zones. When the contacting chambers are located one above the other, the flow rate of the contact substance as it descends from the separation zone, and all the way down to the zone. of the elevator system, is controlled by adjusting the rate with which this substance enters the elevator gas stream from a point below the bed contained in the supply area of the elevator system.

   When the contact substance chambers are located side by side, two such pneumatic conveying systems are provided. According to a preferred variant of the invention, the lifting gas is liable to condensation, being steam for example, and is directed from the separation zone to a barometric condenser where it is condensed in order to create the vacuum. desired.



   The invention will be understood more easily if one refers to the accompanying drawings, in which:
Fig. 1 is an elevational view, partly in section, showing a preferred arrangement of the assembly of the cyclic transformation system according to the present invention;
Fig. 2 is a sectional view taken along line 2-2 of FIG. 1;
Fig. 3 is an elevational view, partly in section, showing a variation

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 te of a part of the transformation chamber of FIG. 1;
Fig. 4 is an elevational view, partly in section, showing details of the feed tank of the elevator system, shown in FIG. 1;
Fig.5 is an elevational view showing a variation of part of the installation shown in Fig. 1;

   and .. ''
Fig. 6 is a similar view of a variant of the feed tank of the elevator system.



   All the drawings are eminently schematic.



   Fig. 1 shows a feed hopper or, separator 10, a transformation or reaction chamber 11, a regeneration chamber 12 and a feed tank 13 of the elevator system arranged in series in the vertical direction. The separator may be of any common known type, the variant shown being of the sedimentation chamber type, where the gas and the contact substance enter from the bottom upwards from the open and flared end of the duct. Elevation 14, located between the upper and lower walls of chamber 10. A cylindrical baffle 15, suspended from the upper wall of chamber 10, terminates near the gas outlet level of the elevator duct.

   A gas outlet duct 16 opens out through the side wall of chamber 10, near the upper end of the latter, and puts the upper part of this chamber in communication with a barometric condenser 130. Cooling is supplied to this condenser through conduit 131, uncondensed gas being drawn through conduit 132 to an ejector 133. A barometric conduit 134 runs downward from the condenser to terminate in a well appropriate, not shown. The barometric condenser can be of standard construction.



  Two vertical feed tubes 17, 18 run downward from the lower end of chamber 10, to terminate at the top of sealing hoppers 19 and 20. The feed tubes meet each other. extend downwards, in the form of tubes 21 and, 22, from the bottom of the sealing hoppers, to end in the upper part of the transformation chamber 11. Sealing gas inlet conduits 23 and 24 open into the upper parts of the sealing hoppers 19 and 20 respectively. The tubes 21 and 22 are closed at their lower ends, except for central orifices 25 of dimensions such as to allow the passage of only part of the total current of the circulating contact substance.

   A series of branch pipes 27 'and 28 extend downward from the tubes 21 and 22, resulting in a series of points distributed evenly over the cross section of the chamber 11. Although the only two gravity feed conduits have been shown, it goes without saying that any desired number can be provided, 4 for example, one in each sector corresponding to one. quarter-circle, in order to ensure a better distribution of the contact substance.



   The transformation chamber 11 shown in the drawings is circular in horizontal section, but can have any other desired shape. A vertical duct 30 extends in a central position through the transformation chamber 11, the open ends of this duct being welded to the upper and lower walls of this chamber, so as to form a central vertical column passing through said chamber. . Dispensing cones, provided in the upper part of the transformation chamber, are supported in a central position below the tubes 21 and 22 respectively by suitable means, not shown. Injection or sprinkling nozzles 34 and 35 are arranged below the cones 32 and 33 and are mounted on the liquid inlet tubes 36 and 37 respectively.

   Nozzles are disposed above the lower ends of tubes 27 and 28, of. so that the liquid charge of oil is injected into the downward flow of contact substance falling from cones 32 and 33 above the surface of the compact bed of contact substance 40. A conduit 41 terminates in the water part. - lower of chamber II and is used for the steam inlet
It will be understood that other suitable arrangements may be

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 provided for the introduction of the contact substance and the hydrocarbons into the transformation chamber. An alternative arrangement is shown in FIG. 3, where. the same elements bear the same reference numbers.



  In the arrangement shown in FIG. 3, the tubes 21 and 22 are fully open at their lower ends, the tube 22 being the only one shown. This latter tube delivers the contact substance over a cone 65, from where it falls into a funnel 66. The contact substance then pours the lorig from the cone 67 into the funnel 68 and; ,, finally, into a tank 69, from where it flows through the tubes 70 onto the surface of the bed. The liquid feed is injected from the nozzles 71 into the contact substance stream flowing over the cone 65. In this system, the contact substance stream is presented entirely as a compact stream.

   Such an arrangement is described in detail in U.S. Patent 2,438,261, issued March 23, 1948.



   Transversely to the lower part of the chamber 11 are provided two horizontal partitions 43 and 44, spaced vertically. A series of upright tubes 42 (not shown) extend upwardly through the upper partition 43. The tubes 42 are distributed evenly around this partition and are closed only at their upper ends. On each tube 42 are fixed inverted collecting cups 45 of conical shape, spaced vertically.

   The lower faces of the cuvettes 45 communicate with the interior of the tubes 42 through orifices 46. From the lower partition 45 lead downwards two funnels 47 and 48 of annular shape, provided with descent chutes 49 and. 48, which start respectively from their lower parts. A plan view of these funnels is shown in Fig. 2. A series of tubes 52 run downward from partitions 43 and terminate at a common level, just above; . annular funnels.



  The tubes 52 are distributed uniformly over the horizontal surface of the partition 43, one half of these tubes supplying contact substance to the funnel 47, while the other half feeds the funnel 48. This arrangement ensures a uniform flow of water. contact substance through all tubes 52, va. that this flux is presented as a compact current which will be throttled at a level situated even lower in the system, as will be described below. The downcomers 49 and ¯50 bring the contact substance to the upper end of the regeneration chamber 12.

   Optionally, it is possible to provide four sets of funnels and descent chutes, instead of two sets, in which case the sets are preferably offset 90 relative to each other. Purge gas inlet manifolds 58 and 59 are provided around the chutes 49 and 50, the latter being provided with louvers 60 to allow the entry of the purge gas. Supply tubes 61 and 62 lead to manifolds 58 and 59, respectively. A vapor outlet duct 64 is connected to the transformation chamber at a level situated between partitions 43 and 44. The arrangements described above and aimed at extracting the catalyst and purging can be replaced by others.

   For example, an alternative arrangement that could be employed is described in U.S. Patent 2,434,202, issued; January 6, 1948.



  When all of the oil feed is in the gas phase, the flow of the reaction mass through the contact substance can be directed from the bottom up, instead of from the top down. Note that the invention is not considered to be limited to the particular construction of the reaction chamber described above, and that other suitable reaction chamber arrangements, known in the art, may be employed. , while remaining within the framework, taken in its broadest sense, of the present invention.
In the upper part of the regeneration chamber 12 is provided a horizontal partition 75 which determines an upper chamber 76.

   A series of evenly distributed tubes 77 run downward from partition 75 and serve to flow the contact substance from the upper chamber as well as to provide a gas space 78 above the column. 79 in the regeneration chamber. An annular type gas intake manifold 80, supplied from conduit 81, is provided in gas space 78.



  Tubes 82, extending downward from manifold 80, terminate in flared lower ends located at an intermediate level in chamber 12.

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  A partition 85 extends through the lower part of the chancre 12, while upright tubes 86, similar to the tubes 42 provided in the reaction chamber, run upwards from the space below. of the partition 85, to end at a level located above this partition. Upturned collecting cups 87 are provided on the tubes 86. A gas outlet duct 88 provides communication between the space below the partition 85 and a chimney 89. Another gas outlet duct 100 is connected between the space located under the partition 75 on the one hand and the chimney 89 on the other hand.

   Funnels 90 and 91, of annular shape, provided with descent chutes 92 and 93 respectively; run downwards from the lower part of the chamber 12 and are supplied with solid material by the tubes 94 which run downwards from the partition 85. The arrangement is similar to that which has been provided for the discharge. of the contact substance in the reaction chamber Il¯, described above. Heat transfer tubes 95 are provided on a same level along the lower part of the regeneration chamber. A suitable heat exchange agent is supplied to these tubes from a manifold provided on one side of this chamber, this agent being discharged to a second manifold provided on the opposite side of the chamber.



  The intake manifold is designated by 96; it is fed back and forth from the intake duct 97. The regeneration gas, for example air, arrives from a blower 98, passing through a suitable passage heater 99, and then goes to through conduit 81 to annular manifold 80. Optionally, heater 99 can be bypassed in some operations. It should be noted that the regeneration chamber described above represents only one of the many possible constructions which are particularly suitable for operations in which a catalyst bearing carbon deposits:

     must be regenerated by combustion 'of these. In operations in which the regeneration chamber is intended only to boost heat exchange by adduction or abduction of heat with respect to the contact substance its construction may s 'deviate considerably from that shown in FIG. 1, this in accordance with the specific requirements of the proposed transaction
The downspouts 92 and 93 deliver the contact substance to the upper part of the supply tank 13 of the elevator system, which is in communication, \) through vents, either with the atmosphere or by through a tube 101, with a low pressure zone.

   Optionally, decompression chambers can be provided along the tubes 92 and 93, above the supply tank, instead of providing vents for this tank. such an arrangement is shown in FIG. 5, where tubes 92 and 93 terminate inside decompression chambers 210 and 211. Gas is vented from the upper portions of these chambers, and the contact substance is directed downwardly through tubes 92 ' and 93 ', to the closed supply tank 13' of the elevator system.

   Hermetic conduits for the contact substance, constituted by the tubes 92 'and 93', allow the feed stream of lift gas to be introduced into the upper part of the reservoir 13 'through the conduit 215.



   The role of the feed tank will be clearly understood by considering FIG. 4 together with FIG. 1. A vertical elevation duct runs upward from a point in the reservoir 13 below the surface 102 of the bed contained in this reservoir, this duct passing through columns 103 and 30 which pass through it. the regeneration chamber and the reaction chamber, and ending in the separator 10, where it terminates at an intermediate level at the ends of this separator.

   The columns 103 and 30 have a diameter substantially greater than that of the riser tube 14, so as to avoid tensions due to thermal expansion and to allow the replacement of a riser tube by another, of larger diameter, \ ) in the event that a greater flow rate of the circulating contact substance is subsequently required for any momept. The lower end of the tube 14 is flared, and the conical cap 104 of a cylindrical intake manifold 105 penetrates from below into this flared end of the tube 14 and occupies a central position therein, so as to leave an annular passage 106 for the entry of the contact substance.

   The collector 105 is connected to the bottom of the

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 reservoir 13 and is supplied with gas through the tube 107. The cap 104 has numerous perforations 108, to allow the introduction of gas into the tube 14. Optionally, the cap 104 may be constituted by screens.



  In the variant shown in FIG. 4, the perforations provided in the cap -: 1.04 are all located above the lower flared end of the riser tube 14; so that the gas from tube 107 enters the riser tube without having to pass through any part of the bed contained in the feed tank. The number and dimensions of the perforations 108 are preferably sufficient to limit the linear velocity of the gas stream passing through them, to the same order of magnitude as the velocity of the gas stream mixed with the contact substance and flowing through it. the tube 14 above the lower flared end thereof.

   Ring-shaped angles 109, 110 and 111 are provided on three levels around the inner periphery of the tank 13. Element 109 serves to throttle the flow of contact substance, while elements 110 and 111 serve. as gas distributors supplied respectively by conduits 112 and 113.

   The gas distributor elements should be located at levels close to that of the lower end of tube 14. Flow control valves 114 and 115 are provided in conduits 112 and 113, respectively, the latter being connected. through line 116 to one side of a three-way valve 117. Line 107 establishes communication between manifold 105 and another side of valve 117 with gas supplied to the third side of valve 117 through the valve. Line 118o A flow control valve 119 'controlled by a diaphragm is provided on line 118 upstream of valve 117.

   The valve 119 is actuated by the flow regulator 120 under the influence of changes in the flow of gas, measured at the port 121.



   The process according to the invention is carried out as follows: the contact substance flows downwards in the form of a substantially compact column through the supply conduits 17 and 18 to the hermetically sealed areas 19 and 20, and from there to the reaction chamber 11. The gravity feed conduits are long enough to provide at their lower ends a column of contact substance exerting a pressure greater than the pressure difference between the chamber. reaction chamber and the recharging hopper 10. Steam or combustion gas, or any other suitable gas forming a hermetic seal, is introduced into the hermetically sealed zones so as to maintain a sheet of inert gas in the vicinity. of the lower ends of the power columns.

   Some of the contact substance passes through the orifices 25 and flows over the cones 32 and 33 and then falls as rain on the surface of the column of material 40. When treating a liquid feed, this can be injected using nozzles 34 and 35 into the rain of contact substance. In the case of a gas-shaped charge, this is introduced through the elbow 41. The remainder of the contact substance flows in the form of compact streams through the tubes 27 and 28, to the surface of the tube. column 40, thus maintaining this surface at a constant level.

   In other arrangements. \) Such as that of FIG. 3, all of the contact substance forming the feed mass can be directed from hopper 10 to column 40 in the form of one or more compact streams. The fluid reaction substance is converted into gas-like products, which are collected by collectors 45 and discharged from the reaction chamber through line 64. The spent contact substance flows in the form of one or more streams. compacts from chamber 11 to chamber 12 and then proceeds therethrough as a compact column of granules descending by gravity.

   Inert purge or purge gas is passed through tubes 49 and 50 in order to rid the contact substance of the gas-like hydrocarbon materials and to prevent reaction gas flow between chambers 11 and 12. The purge vapor can be discharged through line 54 together with the carbonated products; a suitable regeneration gas enters chamber 12 through line 81, manifold 80 and tubes 81 and then rises in part through column 79 to outlet 100, while another part of this gas descends through column 79 to exits 88.

   Regeneration gas

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 ration can be simply a heating or cooling gas, in the case of pyrolysis processes, while dock. 7. can be an oxygen-containing gas capable of burning carbonaceous deposits on the contact substance, in the case of most catalytic processes. Additional heat can be introduced into or removed from column 79 by means of heat exchange tubes 95. The regenerated contact substance descends. by gravity, in the form of compact streams, into the feed tank 13, where it discharges onto the surface of the substantially compacted bed 102.



  The reservoir 13 is provided with a vent at 101, so that the surface of the bed 102 is subjected substantially to atmospheric pressure. Steam is admitted from line 118, through valve 117 and line 107, into manifold 105 and from there upward through perforations 108 to enter annular passage 106 directing upwards and terminating at the lower end of the riser tube 14. This vapor, can be under a relatively low pressure, close to atmospheric pressure, as it is drawn upwards through the tube. 14, can enter the hopper 10, which is maintained under a considerable vacuum.

   A stream of secondary or feed steam is directed from the three-way valve 117 to the tubes 112 and 113 and enters the bed under the distributor 110 or 111 or both, and then passes transversely through the tube. bed of contact substance to terminate in annular passage 106. This causes or forces the contact substance to be entrained in the first gas stream, (i.e., the vertical riser stream) which enters the tube d The elevation 14 without crossing the lito This first stream of gas imparts additional energy to the contact substance and accelerates it until imparting an appropriate rate of elevation.

   It has been found that the flow rate of the contact substance from bed 102 and entering riser tube 14 can be partially or partially controlled. entirely by adjusting the rate of the secondary feed stream o This secondary feed stream should preferably be introduced at one or more points, where it will be forced to flow transversely through the entire bed of substance. contact pressure in the supply tank in an approximately horizontal direction, before reaching the riser tube.

   However, it is believed that the scope, taken in its broadest sense, of the present invention encompasses the fact that the secondary feed stream may be introduced above the surface of the bed, such as through tube 215. in Fig. 5, and can then be caused to flow downward through the bed and then enter the riser tube.



  This latter variant represents a less advantageous embodiment of the invention and, when such an operating mode is adopted, the pressure exerted in the supply tank may be greater than the atmospheric pressure of the amount required to force the secondary feed stream to pass from top to bottom the bed of contact substance in the feed tank of the elevator system. Further., In less advantageous embodiments of the invention, the secondary gas feed stream may be introduced into the bed at one or more points located slightly below the level of the lower end of the tube. gas lift.

   However, in applying the latter methods, care should be taken to avoid substantial boiling or thinning of the bed in the feed area of the elevator system. It is preferred to introduce the secondary feed gas stream at a point which is not substantially below the level of the lower end of the riser tube. In any event, the secondary feed stream must pass through at least an appreciable thickness of the compact bed of contact substance in the feed tank before reaching the lower end of the riser gas tube.



  It has also been observed that it is important to limit the flow of gas and contact substance, at the inlet of the riser tube, to a speed which does not appreciably exceed that reached by the gas and the substance. contact, respectively, in the riser tube above this inlet. Thus, it is desirable that the area exhibited by the perforations 108 not be significantly less than the horizontal free section of the riser tube at a level above the lower flared end of this tube. In addition, the horizontal free section of the annular passage-106 must also be of

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 same order of magnitude as that of the riser tube above the lower flared end thereof.



   A variation of the feed tank for the elevator system is shown in Fig. 6. In this Fig, the elevator tube 14 is not vented at its lower end; and the first gas stream or main gas stream is introduced into the reservoir 13 through the conduit 190, which is aligned with the tube 14, but terminates a short distance below it, so that there remains a vertical gap between the tubes 14 and 190, in which gap the contact substance is supplied or discharged by the stream of secondary feed vapor coming from the tube 191.

   It has been found that when the vertical gap between the ends of tubes 14 and 190 is sufficiently short, the gas which rises from tube 190 prevents the formation of a compact bed of any size in this gap, so that the gas from tube 190 actually passes between the ends of tubes 190 and 14 "without having passed through a compact bed of somewhat considerable thickness in the feed zone".

   It should be noted that the passage highlighted above, as well as passages which express the same idea and which are used herein in the description and claims of the present invention, are intended to cover, in the sense of the. The wider process illustrated by Fig. 1, where the first gas stream is introduced directly into the first riser tube at a point above the lower end thereof., as well as the process. illustrated by FIG.

   6 where the first gas stream is introduced into the supply zone at a point below the lower end of the riser tube and separated from this end by a small gap, as described above. . The actual dimensions of the gap depend on the dimensions of the tubes 14 and 107. For example, when the tubes 14 and 190 have respective diameters of ten inches and seven inches (25.4 cm. And 17. ) 78 cm.), It has been found that a vertical gap of two to ten inches (5.08 cm. To 25.4 cm.) Provides satisfactory operation.

   To ensure that the linear velocity of the gas coming from the tube 190 will not be substantially greater than the velocity of the mixture of gas and contact substance in the tube 14, it is preferable to replace the arrangement according to FIG. 6 by the arrangement according to FIG. 4, modified in the direction of lowering the level of the conical head 104 relative to the lower end of the tube 14, so that all or part of the perforated area of the head 104 is located below the level, of the lower flared end of the riser tube 14. In the variant of Fig. 6, the contact substance does not have to flow from the bottom upwards before being entrained by the flow of riser gas,

   unlike the variant of FIG. 4.



   With respect to pin 1, the contact substance rises through tube 14 to enter hopper 10, where it is deposited as a result of the reduced gas velocity in this hopper. The separated steam goes through line 16 to barometric condenser 1309 where it condenses on contact with water, thus creating a vacuum by suction in hopper 10. Water and condensed steam leave condenser 130 through barometric pipe 134.

   As a vapor atmosphere is maintained inside the lower portion of the supply tank, only a very small amount of uncondensed gas enters the lift gas stream, * however, any amount of non-condensable gas that would be drawn in in the system could be evacuated from the barometric condenser by a small compressor or an ejector 133. The vacuum maintained in the hopper 10 should be large enough to determine an elevation of the contact material through the tube 14 and to overcome the pressure drop. through tube 14.

   In general, the pressure drop across tube 14 can be on the order of 3 to 12 1bs. per square inch (0.211 kg / cm2 to 0.844 Kg / cm2), depending on the flow rate of the contact substance, its density in the riser tube, the length of the riser tube and the gas flow rate. To ensure proper control of the lifting operation, the vacuum in chamber 10 must be kept constant. A suitable method of achieving this is to introduce a small quantity of non-dondensable gas through the tube 140 into the con-

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 barometric density. The flow of gas through tube 140 is controlled by valve 141 and a pressure monitor 142, in order to keep the vacuum in hopper 10 constant.



   The level of the contact substance is kept constant in the separator 10 by the fact that a small portion of the circulating mass can overflow into the funnel 200 from where it goes through the tubes 201 and 300 towards the upper part. of an accumulator 204. The contact substance is maintained at levels within relatively narrow limits in the lower part of the accumulator, these levels being measured by the level indicator 301. Circulation continues in the ring system results in slight attrition of the contact substance. The substance transformed into fines can be removed from the system by passing part of the mass of this substance through tubes 201 and 305 into a separator-scrubber 202, where this substance is purified and freed of fines by an ascending gas stream.

   The gas containing the fines is directed to a separator 203, where the separation of the fines takes place. The purified granular substance settles in the accumulator 204, from where it flows through a tube 205 to the supply tank 13 of the elevator system.



   To avoid exaggerated fluctuations in. the operation of the barometric condenser, as well as to ensure proper separation of the contact substance and the gas in the hopper 10, it is advantageous to keep the gas flow rate constant in the tube 14, regardless of the flow rate of the gas. contact substance in circulation. In addition, it was found that he was advanced. It is important to maintain the linear velocity of the gas in the riser tube, so as to achieve relatively narrow optimum flow limits, in order to ensure the transport of the contact substance with a minimum of attrition losses.



  It has been found that this can be achieved by adjusting the total flow rate of the vapor stream so as to keep it substantially constant, by means of the control valve 119. The flow rate of the contact substance entering the vapor tube. The elevation is controlled by adjusting the gas flow rate through tube 112 or 113 or both, which are fed from tube 116. Any adjustment of gas flow through tube 116 is compensated by a setting substantially equal and opposite, of the flow through the tub, e 107. This can be done with the three-way valve 117 or by any other suitable means.

   Although the preferred embodiment of the present invention involves the use of a suction-type lifting system, to transfer the contact substance from the mass of the bed formed in the feed tank to the hopper. charging., it goes without saying that the particular method described here and aiming at the introduction of the contact substance into the lifting gas stream and the adjustment of the flow rate of this substance is not considered to be limited to the systems. suction lifts, but can be used where the recirculation hopper is maintained at a pressure close to atmospheric pressure, while the lift gas is supplied to the lower end of the lift system at a pressure sufficient to ensure transport of the contact substance.

   



   According to a preferred embodiment of the present invention, the reaction chamber is located a short distance above the regeneration chamber., And the latter is located a short distance from the ground level, while a The relatively small refill hopper is located a significant distance above the reaction chamber. This allows all large chambers to be located close to ground level, saving the cost of steel going into the construction. It is advantageous to maintain the pressure in the regeneration chamber at a value which is not appreciably higher than that of the pressure in the reaction chamber, so that it is sufficient to provide a low height of the column of the regeneration chamber. contact substance to ensure gravity flow between the two chambers.

   This can be done with the aid of a diaphragm actuated valve 160 controlling the chimney 89, as well as with the aid of a differential pressure regulator 1610 It should be noted that as the tank 13 of the lifting system is maintained at a pressure close to atmospheric pressure, the tubes 92 and 93 can

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 also have a relatively short length, so that practically the entire height of the gravity feed column ,,, which remains in this system, is located in conduits 17 and 18.

   It is evident that a continuous and uninterrupted compacted current of contact substance extends from the hopper 10, through the conduits 17 and 18 and the tubes 27 and 28, to the column 40 of the reaction chamber and, from this latter column, and through tubes 49 and 50, to column 79 contained in the regeneration chamber, and then from this latter chamber, through tubes 92 and 93, to compact bed 102 located in the feed tank 13.

   The flow rate of the solid material flowing from top to bottom through the whole of this system is controlled only by adjusting the flow rate of the contact substance circulated from bed 102 and introduced into tube d. 'elevation 14, the latter flow being in turn controlled by the adjustment of the flow of gas coming from the distributors 110 and 111 and passing through the bed 1020 However, it goes without saying that the particular method' described here and aimed at controlling the flow with wherein the contact substance is introduced into the rising gas stream while maintaining substantially constant the total gas velocity in the riser tube, is not to be construed as being limited to its application to the particular case including the relative positions of the reaction chamber and regeneration chamber,

   as described above. In some constructions the two chambers may be arranged side by side and two separate gas lift systems may be employed. Further, and although it is preferable to employ steam as the lift gas, the invention contemplates the possibility of replacing this with other condensable gases. For example, condensable hydrocarbon vapors can be used as lift gas and be recovered from a well located at the base of barometric conduit 134.



  In some operations, the gas supplied to the supply tank and drawn into the riser tube may be a non-condensable gas in which case the barometric condenser may be replaced by a vacuum pump or other suitable apparatus to allow for evacuate the separator 10.



   As an example of the operation of the method and apparatus according to the present inventions, consideration will be given to the application thereof to a catalytic de-cracking process using a synthetic silica-alumina catalyst in the form of globules of 4-20 stitches (Tyler series). In a typical operation, the feed hopper 10 is located 185 feet (one foot = 0.3048 m.) Above ground level, and is maintained under a vacuum corresponding to approximately 7 square lb- resparpouce (live per inch - 0.0703 kg / cm2). This vacuum is kept substantially constant by regulating the operation of the barometric condenser 1300. Air or combustion gas can be introduced for this into the condenser through tube 140.

   The catalyst at a temperature of about 1100 F (593 C) descends through tubes 17 and 18 to the reaction chamber, where it is contacted with a reduced charge of crude oil supplied through tubes 36 and 37 .. A charge of vaporized diesel is supplied through line 41.



  The upper part of the reaction chamber is maintained at a pressure of about 10 pounds per square inch while the pressure of the steam in hoppers 19 and 20 is maintained at a value which exceeds the previous one by about half a pound. .. The vertical distance between the bottom of the hopper 10 and the sealing hoppers 19 and 20 is approximately 90 feet. Ducts 21 and 22 are only a few feet in length. The spent catalyst passes from the reaction chamber to the regeneration oven through conduits 49 and 50, which are only about six feet long.

   The effective pressure at the outlet of the reaction chamber is about 7 pounds per square inch while the effective pressure in the chimney 89 may be. maintained at about 6 pounds per square inch. Optionally, the pressure in the stack can be allowed to drop to substantially atmospheric pressure, but it is not appropriate to allow it to rise substantially above that prevailing in the reaction chamber, since this would require an increase in the length of the gravity flow conduits 49 and 50, and \) therefore results in an undesirable increase in the overall height of the whole assembly.



  The catalyst is regenerated in the oven by the combustion of the impurities, and the temperature of the catalyst is set to a value of approximately 1200 F (649 C).

 <Desc / Clms Page number 12>

 by the single series of cooling tubes 95. The flow rate of the circulating catalyst is maintained at about 2.5-4.5 parts by weight of catalyst per part of the oil charge going to the reaction chamber, while the overall flow rate of the oil feed is on the order of 1.0 to 2.0 volumes of oil per hour, measured at 60 F (15.6 C) per volume of catalyst in the reactor.

   Under these conditions, the catalyst can be regenerated without its temperature rising to a value liable to determine heat damage, this result being obtained by the use of cooling tubes with one or two stages only in the lower part. regeneration oven The regenerated catalyst goes under. the form of a compact stream from the oven to the feed tank 13 of the elevator system, the distance between the bottom of the oven and the top wall of the feed tank being only 6 feet approximately.

   When the lifting system is suctioned, the pressure prevailing in the upper part of the tank 13 is substantially equal to atmospheric pressure, while the pressure which prevails in the lower part of this tank, near the inlet of the tank. riser tube can be controlled at any point between limits ranging from a vacuum of several pounds per square inch to an effective pressure of 1 or 2 pounds per square inch. The depth of the bed above the lower end of the riser tube 14 should be in the range of 3 to 8 feet.

   The levels of the gas inlet fittings 112 and 113 to the reservoir 13 should preferably be, relative to the flared lower end of the riser tube 14, at distances of between 1 and 2 feet, although in less advisable installations, the secondary gas supply can be made entirely at a point above the bed situated in the supply tank. The steam is introduced into the supply tank 13 of the lifting system through conduits 107 and 116, the ratio between the feed or secondary vapor and that which is introduced directly into the riser tube being controlled in order to maintain the circulation of the catalyst at a required rate.

   To ensure a circulation of about 60 tons per hour, in which the catalyst is elevated about 180 feet, a riser tube with a diameter of 10 inches is sufficient, while the flow of exhaust vapor to The low pressure required for the lift is about 40 to 50 pounds per minute for a granular catalyst having a packed bulk density of about 45 pounds per cubic foot. It should be noted that by means of the method according to the present invention, the first or primary stream of lift gas is supplied to the riser tube without having to pass through a substantial thickness of the bed of contact substance.



  The linear velocity of this gas stream as it enters the lower end of the riser should not be appreciably greater than the velocity of the mixed stream of gas and contact substance flowing through the riser. riser tube above this end. In general, the linear velocity of the first gas stream should be at least within the limits of 0.5 to 2.0 times the maximum linear velocity of the mixed stream of gas and contact substance through the riser tube. above the lower flared end thereof.

   The velocity of gas and catalyst in annular passage 106 of FIG. 4, or around the lower end of tube 14 in FIG. 6, should not be significantly greater than the speed in the lifting tube a short distance above the flared lower end thereof.



   Thus, the extremely high gas velocity in the feed zone, which has been renounced in earlier systems which could be referred to as "jet feed elevation systems" is avoided by the following method the present invention. In addition, since the first gas stream directly enters the riser tube without having passed through any substantial part of the contact substance bed, turbulence of the contact substance stream and the flow at contact are avoided. high speed, which is found in gas lifting systems used today.



   In a large number of operations, this first gas stream or primary stream may constitute the major part of the total gas supplied to the riser tube.

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   Generally speaking, the proper gas velocity to be maintained in the riser tube will vary depending on the particular gas and contact substance present, the pressure and temperature of the riser9 as well as the temperature. length of elevation path In general, the linear velocity of the upward flow of gas through the riser tube should be within the range of about 3 to 60 feet per second, but should be preferably raise to 10-40 feet per second above the final velocity of the contact substance particles.

   For example, in a suction type lift system, in which air at about 900 F (482 C) is the lift gas, and in which the contact substance is a synthetic silica catalyst. -alumina in the form of spherical globules of a gauge corresponding to about 4 to 20 meshes of the Tyler series and of a bulk density in the packed state of 45 pounds per cubic foot, the linear velocity of the gas in the riser tube should be between about 85 and 130 feet per second and preferably be 90 to 100 feet per second, while the linear velocity of the catalyst is within the limits of about 10 to 50 feet per second , but preferably within the limits of 10 to 20 feet per second,

   the absolute pressure of the lifting fluid being 7.7 and 14.7 pounds per square inch respectively at the ends. upper and lower part of this tube. Under the above conditions, a riser tube with an inside diameter of about 14 inches and a height of 180 feet can satisfactorily handle about 95 tons of contact material per hour. The relative amounts of feed or secondary gas and lift gas supplied directly to the riser will vary depending on the rate at which the contact substance is transferred and the dimensions of the gap between the inlet. primary current and the lower end of the riser tube.

   In general, the side stream can amount to about 5-90 percent and preferably 10 to 65 percent of the total gas supplied to the riser. The flow rate of the secondary gas stream must anyway be less than the value at which this gas could produce "vent" or "bubbling" of the contact substance bed. For the reasons set out above, it is preferable to set the overall gas flow rate at a constant value and to compensate for any change in the flow rate of the secondary gas stream by an equal and opposite change made to the other neck. - rant, which enters directly into the riser tube through duct 107.

   Considering the scope of the present invention in its broadest sense, it can be envisioned that it also covers the fact that the rate with which the catalyst enters the riser tube can be controlled by adjusting the rate. gas supplied through tube 112 or 113, or both, while the current entering through tube 107 is adjusted at the same time, if necessary, to maintain the density of the catalyst in the riser tube within the limits of about 3 to 24 pounds per cubic foot, but preferably within the range of 4 to 10 pounds per cubic foot, using as a base a catalyst having a normal bulk density in the packed state of about 45 pounds per cubic foot. -
Through the employment of a.

   suction-type lifting system, making use of a condensable lifting gas, not only significant savings are achieved due to the elimination of the gas compressor required in conventional pressure lifting systems, but also a reduction of the total amount of lift gas? Steam, for example, required to elevate the contact substance as compared to the amount required in pressure elevation systems.

   For example, when a sufficient vacuum is maintained in the separation zone 10 to lift the contact substance from a supply tank 13 subjected to a pressure close to atmospheric pressure, the necessary amounts of lifting vapor are required. reduced by about a third of that which would have been necessary to raise the same quantity of contact substance to a separation zone subjected to atmospheric pressure, from a supply zone of the system elevator maintained under sufficient pressure to ensure elevation of the contact substance.



   It should be noted that the particular details of the construction of the apparatus and the operating conditions, as well as the examples by-

 <Desc / Clms Page number 14>

   Particulars of the application of the present invention cited above are to be regarded as illustrative and should not be regarded as limiting the scope of this invention, except to the extent that the latter is limited by the following claims.



   CLAIMS.



   1 - In a continuous process for the transformation of hydrocarbons, in which a granular contact substance is caused to pass in a cyclical manner through contacting zones, one of which constitutes a delimited transformation zone, in which this substance comes into contact with a liquid hydrocarbon in order to effect its transformation into gasiform products, the other contacting zone being a delimited regeneration zone in which the contact substance is subjected to the action of a suitable regenerator gas intended to regenerate it - with a view to its reuse in the said transformation zone:

   the improved method for transferring the contact substance from one of these contacting zones to the other, and which consists of: passing this substance downwards, from one of said contacting zones, to 'to a substantially compact bed of said substance;, maintained below this zone, in a delimited zone; maintaining a delimited elevation passage extending upwardly from an intermediate point located in this bed, to a point located above the other contacting zone, this passage being in communication. , by .. its lower end opening downwards, with the said bed;

   introducing a first stream of riser gas into said demarcated area so that it can enter the lower end of said riser passage without the gas having to pass through any substantial portion of the substantially compacted bed; introducing a second stream of elevating gas into said bed at a distance from the lower end of said elevating passage and passing it through the interposed portion of said bed into the end lower portion of said elevation passage, thereby causing contact substance forming part of said bed to integrate with said first stream;

   raising the contact substance suspended in the mixed gas streams, through said elevation passage and up to said point above said other contacting zone, and passing this substance from this last point up to said other contacting zone; and controlling the rate of contact substance entering said elevation passage, controlling the rate at which said second stream of elevating gas is introduced into said bed.

** ATTENTION ** end of DESC field can contain start of CLMS **.


    

Claims (1)

2 - Improved method for bringing a granular solid substance into an upwardly extending air passage through which it is elevated by an elevating gas to a high receiving zone, this method consisting of: maintaining a substantially compact bed of said contact substance around the lower end of said elevation passage and in communication with the interior of said passage along the lower end, opening downward, of this elevation passage; continuously pouring contact substance onto the surface of said bed; delivering a first stream of lift gas to the lower end of said lift passage without forcing said gas to pass through any substantial thickness of said bed; introducing a second stream of lift gas into said bed at at least one point a substantial distance from the lower end of said passage; and in passing said gas through the interposed part of said bed and then into the lower end of said elevation passage, this with a sufficient flow rate to force the solid material to integrate into said first stream of gas, so that it is suspended in the mixed gas stream which flows through said passage; and adjusting the rate at which said second gas stream is introduced, to control the introduction of solid material into said passage and to the required rate; and maintaining the linear velocities of said first and second riser gas streams, at their point of entry into the riser passage, at a value not substantially exceeding the linear velocity of the mixed gases in the passage of elevation above this entry point. <Desc / Clms Page number 15> 3 = In a continuous process - for the transformation of hydrocarbons ;, in which a granular contact substance is cyclically passed through two contacting zones, one of these zones being a zone process, in which this material flows in the form of an essentially compact column, while being in contact with a liquid hydrocarbon, in order to ensure the transformation thereof into gas-like products, the another contacting zone consisting of a delimited regeneration zone in which the contact substance flows in the form of a substantially compact column ;, while being subjected to the action of a suitable regenerator gas intended to regenerate it in view of its re-use in the said transformation zone: the improved method for transferring the contact substance from one of said contacting zones to the other, 'and which consists of: passing this substance downwards from one of said contacting zones to a substantially compact bed of said contact substance maintained, below this first zone., in a delimited zone; maintaining a confined elevation passage extending upward from an intermediate point in said bed to a point above the other contacting zone said passage being in communication by its lower end emerging downwards, with the said bed; introducing a first stream of riser gas into said bounded area so that this gas can enter the lower end of said riser passage without having to pass the gas through any substantial portion of the riser. substantially compact bed; introducing a second stream of lift gas into said bed at a distance from the lower end of said lift passage; and passing this second stream through the interposed part of said bed, into the lower end of the bed elevation passage, thereby causing the contact substance coming from inside said bed to integrate into said first stream; maintaining the flow rate of said gas stream through the bed below the value which could substantially disrupt the compactness of this bed; raising the suspended substance in the mixed gas of the first and second streams to said point above the other contacting zone; and in lowering the contact substance by gravity to the column contained in said other contacting zone; in maintaining the linear speed with which said first stream enters the elevation passage at a value which does not significantly exceed the maximum linear speed of the mixed gas stream in said passage above the level of the inlet gas in it; and controlling the rate with which the contact substance enters from said bed into the lower end of said elevation passage by controlling the rate at which said second elevation gas stream is introduced. in the said bed. 4 - Improved method for introducing a granular solid substance into: an elevation passage extending from bottom to top. And through .., which this substance is elevated by an elevating gas to a re-zone. - high concept, this method consisting of: maintaining a substantially compact bed of said solid substance around the lower end of said elevation passage and in communication with the interior of said passage along the path. lower end, opening downwards, of said elevation passage; pouring the contact substance continuously onto the surface of said bed; supplying a first stream of elevating gas into the lower end of said elevation passage without causing this gas to pass through any substantial thickness of said bed; in maintaining the linear speed of said stream, as it enters said passage, at the same order of magnitude as the speed of the total gas in the part of the elevation passage situated above this entry; in introducing a second stream of lifting gas into said bed, at least at a point situated at a substantial distance from the lower end of said passage and at a small distance below the level of this end; and passing said second gas stream through the interposed portion of said bed and then through the lower end of said elevation passage at a sufficient rate to incorporate solid into the bed. said first gas stream, so that this is suspended in the mixed gas stream moving in said elevation passage; and adjusting the rate at which said second gas stream is introduced so <Desc / Clms Page number 16> controlling the entry of the solid material into said passage according to the desired flow rate. 5 - Cyclic process for the conversion of hydrocarbons, consisting of: passing a granular contact substance from top to bottom through two delimited and separate contacting zones, arranged one above the l the other in a vertical series circuit, one of these zones being a transformation zone, while the other is a regeneration zone; to introduce a charge of liquid hydrocarbon so as to bring it into contact with said contact substance in the transformation zone, to ensure the transformation of this charge into a gas-like product, to evacuate said gas-like product of said transformation zone; to pass a regenerating gas so as to! placing in contact with the contact substance in said regeneration zone, to ensure regeneration of the contact substance with a view to its reuse in said transformation zone; causing the contact substance to flow downwardly in the form of a continuous, unthrottled and substantially compact current, from the lower of the two contacting zones, to a substantially compact bed of contact substance. tact, maintained in a separate zone below these zones, so as to ensure the maintenance of the compactness of the current of contact substance directing upwards from said bed and terminating at the two contacting zones and crossing these; to complete the filling of the upper contacting zone by causing the contact substance to flow downwards from a supply zone situated a considerable distance above these two zones to the contacting zone upper contact, this substance then forming a delimited and compact column having a sufficient height to ensure the flow by gravity of the contact substance by overcoming the pressure which prevails in the upper contacting zone; to maintain communication between said supply zone and said bed contained in the zone taken up by the lifting current, by means of a vertical delimited passage which opens at its upper end into the said feed zone, while its lower end opening towards the bottom opens onto said bed at a point located below the surface thereof; to maintain a substantial vacuum in said supply zone by continuously evacuating gas from the upper part of this zone, so as to establish a suction acting through said delimited passage and into said bed contained in said pick-up area; causing a first low pressure gas stream to flow, directed substantially directly into the interior of the lower end of said delimited passage, starting from a point outside said bed; passing a stream of take-up gas through at least a portion of said bed, toward the lower end of said passage; then in the interior of said passage, in order to cause the contact substance to flow from said bed into said first stream; in causing the contact substance suspended in the mixed gas streams to flow upwards, through said passage and up to said supply zone, by the traction exerted by said suction ; to ensure the separation of the gas and the contact substance in said supply zone and to control the rate of the circulation of the contact substance by controlling the rate of the said stream of take-up gas through the said bed, in the said pick-up area. 6 - Cyclic process for the transformation of hydrocarbons into products with a lower boiling point, consisting of: passing a granular contact substance from top to bottom through two contacting zones arranged so as to form a vertical series circuit, in which zones the contact substance flows in the form of a substantially compact column and between which zones it flows in the form of a compact, delimited and unthrottled stream of relatively small section, one of said contacting zones being a reaction zone and the other being a regeneration zone; passing a reaction substance in the form of a liquid hydrocarbon, so as to bring it into contact with the contact substance, at a temperature suitable for effecting the transformation of said reaction substance into gas-like products of a lower point e-boiling; in removing said products from said reaction zone; by hand- @ <Desc / Clms Page number 17> maintain an inert gas seal near the upper and lower ends of said reaction zone, so CI. preventing escape of the reaction substance through the substance inlet and outlet streams. of contact; to pass a. regenerator gas suitable for contact with the contact substance in said regeneration zone, in order to effect regeneration of the contact substance with a view to its reuse in said reaction zone; in passing the contact substance from that of said contact zones and which is situated lowest, in the form of an unthrottled and substantially compact current, to the surface of a bed of the said contact substance contained in an elevation support area; located below this last contacting zone; ' passing a delimited flow of lift gas upwardly through at least a portion of said bed to a separation zone located above the upper contacting zone, said flow of lift gas. elevation gas not being in communication with said bed, except at its lower end which opens down into said bed at a point below the surface of said bed and above the bottom of this last; introducing a separate control gas stream into said bed and causing this stream to pass through a portion of said bed and then flow upward from said bed to integrate with said bed. confined rising current, thereby causing the contact substance located near the point of communication between said delimited rise current and said bed to rise into said rise current; in raising the contact substance which is integrated with said raising current from said bed to said separation zone situated above the highest of the contacting zones thus ensuring the separation of the contact substance with the carrier gas in said separation zone; exhausting the separated gas from the upper part of said separation zone; in passing the contact substance downwards from the lower part of said separation zone, in the form of a vertical and substantially compact stream, into the highest contacting zone, this compact stream having a vertical length sufficient to ensure a flow by gravity of the contact substance towards the said highest contact zone and against the antagonism of the pressure prevailing therein; and controlling the rate with which the contact substance flows downward from said separation zone into and through said contacting zones and up to said bed in said pick-up zone, by adjusting the rate with which said separate control gas stream is introduced into said bed contained in said lift-system pick-up zone. 7.- Cyclic process for the transformation of hydrocarbons into products with a lower boiling point, consists in passing a granular contact substance from top to bottom through two contacting zones arranged so as to form a vertical series circuit in which zones the contact substance flows in the form of a substantially compact column and between which zones this substance forms a compacted and unthrottled stream of relatively small cross section, one dice contacting zones being a reaction zone and the other being a regeneration zone; passing a fluid reaction hydrocarbon into contact with the contact substance and at a suitable temperature to effect the conversion of said reaction hydrocarbons into gas-like products of lower boiling point; removing said products from said reaction zone; maintaining an interfering gas seal near the upper and lower ends of said reaction zone, in order to prevent escape of the reaction substance through the inlet and outlet contact substance streams; passing a suitable regenerating gas in contact with the contact substance in said regeneration zone, to ensure the regeneration of the contact substance for its re-use in said reaction zone; passing the contact substance from that of said contacting zones which is situated lowest, in the form of a substantially compact and unthrottled stream. (1) onto the bed surface of said substance. contact area contained in a support area of the elevation system located below the latter contact area; to maintain a delimited passage going from bottom to top from a point in the interior <Desc / Clms Page number 18> the interior of said bed, below the surface and above the bottom thereof, up to a delimited separation zone, situated at a sensible vertical distance above the upper contacting zone, said delimited passage being in communication, by its lower end, with said bed, while being otherwise isolated therefrom; in evacuating the gas from the upper part of said separation zone, so as to maintain the latter under a high vacuum, which has the effect of sucking gas upwards in said delimited passage; introducing lift gas into the lower end of said delimited passage from a point outside said pick-up zone without forcing this gas to pass directly through any major part of said bed; introducing a separate regulating stream of gas into said bed and passing it directly through a portion thereof, before it enters said delimited elevation passage, so as to bring contact substance into it. from the interior layers of said bed to enter said passage and be lifted by gas drawn upwardly through said passage into said separation zone; maintaining the linear speed of each of the two gas streams entering said passage within limits which are about 0.5 - 2.0 of the linear speed of the mixed gas stream in the passage above this bed; separating the contact substance from the lift gas in said separation zone; and causing the separated contact substance to flow downwardly in the form of a substantially compact, unthrottled, gravitational downward stream from said separation zone to the upper contact zone below. of this separation zone; and controlling the rate with which the contact substance flows downwardly from the separation zone to and through the contacting zones, and from the lower contacting zone to the lower contacting zone. to said lifting system take-up zone, solely by controlling the rate with which said distinct stream of gas is introduced into said bed contained in said lifting system take-up zone. 8. A continuous process for the catalytic cracking of fluid petroleum fractions, comprising: passing an adsorbent granular catalyst through a demarcated transformation zone in the form of a substantially compact column; in passing a fluid hydrocarbon fraction in contact with said catalyst, under suitable temperature and pressure conditions, to effect the catalytic cracking of said fraction into a lower boiling point gasified product, the pressure in said transformation zone being greater than atmospheric pressure; removing said carbonated product from said processing zone; in passing an exhausted catalyst carrying a carbonaceous deposit from top to bottom from said transformation zone to a regeneration zone situated below this transformation zone, in the form of a compact stream, of short in length, unthrottled and descending by gravity, while maintaining an inert gas seal preventing the passage of a reaction gas stream between said transformation and regeneration zones; passing the catalyst in the form of a substantially compact column from bottom to top through said regeneration zone, while contacting it with an oxygen-containing gas, in order to burn the deposit carbonaceous of said catalyst; maintaining the pressure in said regeneration zone at a level which is not substantially higher than that prevailing in said transformation zone; in passing the regenerated catalyst downwardly from the lower end of said regeneration zone, in the form of a substantially compact, unstangled and gravitational downward stream, to the surface of a substantially bed. compact catalyst, maintained in a separate zone below said regeneration zone, so as to ensure continuity of a substantially compact catalyst stream extending upwardly from said bed through said compact stream and through them. regeneration and transformation areas; compartmentalizing the lower part of said bed, so as to constitute a gas space in communication with the bottom of said bed; introducing a first stream of vapor into the lower portion of said bed, near said gas space to cause catalyst to rise from the interior layers of said bed and enter said gas space; to introduce a second stream of steam <Desc / Clms Page number 19> in said gas space at a level below the bottom of this space, for mixing with the rising catalyst; sucking the mixture of vapor and catalyst from the bottom upwards from said gas space,, as a bounded stream, into a sedimentation zone located a substantial distance above said transformation zone; ensuring the separation of the vapor and the catalyst in said sedimentation zone; sucking the vapor from the upper part of said sedimentation zone towards a barometric condensation zone, where it is mixed with water in order to ensure its condensation; to control the rate with which the vapor is sucked from said separation zone, in order to maintain the latter under a sufficient vacuum to raise the catalyst from said bed located in said take-up zone, to the said sedimentation zone, from which it descends into the transformation zone in the form of a substantially compacted and unthrottled feed column, while maintaining an inert gas seal near the lower end of said column. the feed, this column having a sufficient height for the pressure exerted by the catalyst at the lower end of this column to be greater than the pressure difference between said sedimentation and transformation zones; controlling the rate at which the contact substance flows downward in the form of the continuous, unstrangled and compact catalyst stream which extends from the settling zone, through the transformation and settling zones. regeneration., up to said bed, in said lift system pick-up area, by adjusting the rate of admission of the aforementioned first stream of steam into the lower part of said bed in said lift system pick-up area ; and controlling the total flow rate of the vapor inlet into said gas space, to maintain the density of the catalyst in the stream of catalyst and vapor rising from the gas space to the gas zone. sedimentation, within the limits of about 3 - 24 pounds per cubic foot. 9. Cyclic process for the conversion of hydrocarbons into lower boiling point products, consisting of: passing a granular contact substance from top to bottom through two contacting zones arranged in a vertical series circuit , in which zones the contact substance flows in the form of a substantially compact column, and between which zones it flows in the form of a compact stream., unobstructed and delimited, of relatively small section, a said contacting zones being a reaction zone and the other being a regeneration zone; passing a fluid reaction hydrocarbon to a suitable temperature to effect the conversion of said reaction substances into gas-like products of lower boiling point; removing said products from said reaction zone; maintaining an inert gas seal near the upper and lower ends of said reaction zone, to prevent escape of the reaction substance through the inlet and outlet streams of the contact substance; passing a suitable regenerating gas into contact with the contact substance in said regeneration zone, to ensure regeneration of the contact substance with a view to its re-use in said reaction zone, passing the contact substance from that of said contacting zones which is situated lower, in the form of an unobstructed stream and substantially compacted to the surface of a substantially compact bed of this contact substance, contained in a zone for taking charge of the lifting system located lower than this last contact zone; maintaining a confined elevation passage extending upwardly from a point situated in the interior of said compact bed, and intermediate between the ends thereof, to a point situated above the upper contacting zone, said passage being in communication, by its lower end opening downwards, with said bed; directing a first stream of elevator gas into the lower end of said elevation passage, without forcing it to pass through a substantial thickness of said compact bed; introducing a stream of take-up gas into said bed at a distance from the lower end of said elevation passage and passing it through the interposed portion of said compact bed, to terminate it in -the lower end of said passage of- <Desc / Clms Page number 20> elevation, thereby causing contact material from said bed to integrate into said first stream; raising the contact substance suspended in the mixture of the first lift gas stream and the charge gas, through said elevation passage to said point above the pick-up zone. in upper contact; and allowing the contact substance to descend by gravity from said point onto the column contained in said upper contacting zone; maintaining the linear speed of the first gas stream, as it enters said passage, within 0.5 to 2.0 times the maximum speed of the mixed gas along that passage; and controlling the flow rate of the contact substance as it enters said riser passage, by adjusting the rate of introduction of said second riser gas stream into said bed. 10. In a cyclic process for the transformation of hydrocarbons in the presence of a moving solid granular substance, in which the solid substance is directed in a cyclic fashion through two contacting zones, one of these zones being a transformation zone, in which this material is brought into contact with fluid hydrocarbons subjected to a reaction, the other zone being a regeneration zone, in which this way is contacted with a suitable regenerating gas, to be regenerated with a view to its reuse in said transformation zone, the improved method of transfer of contact substance from one of said zones to the other, consisting of: in passing the solid substance from one of said contacting zones to a substantially compact bed of this solid substance, contained in a support zone of the lifting system; in maintaining a limited flow of lifting gas s 'extending upward from a point in the interior of said bed, below the surface thereof, to a separation zone located above the other of said contacting zones, said bounded lift gas stream being in communication with said bed below the surface thereof; introducing a first stream of lift gas from outside said pick-up zone to the lower end of said limited lift gas stream, passing a stream of control gas through a part of said bed, towards the point of communication of said bed, with said delimited lifting gas stream; and then allowing the second gas stream to integrate and mix with said lift gas stream so as to cause solid substance from the inner layers of said bed to enter said bed. lifting gas stream; maintaining the total amount of gas admitted into said lift gas stream at a suitable and substantially constant rate which is suitable for raising the contact substance from said pick-up zone to said separation zone; to ensure the regulation of the flow rate of the introduction of the solid substance into the said lifting gas stream, by adjusting the flow rate of the said regulating gas stream, while maintaining constant the total flow rate with which this gas propagates, in said rising gas stream, compensating for any equal and opposite adjustment made to said regulating gas stream, by an equal and opposite adjustment made to the rate at which gas is admitted to form said first stream gas going to the lower end of said lift gas stream; ensuring the separation of the contact substance from the lift gas in said separation zone; and passing the separated contact substance to the other of said contacting areas. 11 - In a cyclic process for the transformation of hydrocarbons in the presence of a moving granular solid substance, in which the solid substance is made to pass in a cyclic fashion through two contacting zones, one of these zones being a transformation zone, in which this material is brought into contact with fluid hydrocarbons subjected to a reaction, the other zone being a regeneration zone, in which this substance is brought into contact with a gas suitable regenerator, to be regenerated with a view to its re-use in the said transformation zone, the improved method for ensuring the circulation of the said solid substance, consisting of: in passing the solid substance from one of the said contacting zones to a substantially compact bed formed by the said <Desc / Clms Page number 21> solid substance in a lifting system pick-up area; maintaining a delimited elevation passage extending upwardly from a point in said beds at a substantial distance below the surface thereof: and above the bottom of this lita up to a zone of separation of the solid material and the gas, situated above the other of the said contacting zones, the lower end of the said passage, opening towards the bottom and located in the interior of said lite being at least partially open - '. to allow communication between said bed and said elevation passage) '. introducing a first stream of gas from outside said lift system pick-up area, into the lower end of said passage, without forcing this gas to pass through any significant portion of that bed; introducing a second rising gas stream into said bed some distance from the lower end of said passage and passing the gas through the bed and then into the lower end of said passage. - lesson in bringing the solid substance to integrate into said first gas stream and to be elevated by the mixed upward streams of gas through said passage and into said separation zone; to ensure the separation of the solid substance from the gas in said separation zone; in evacuating the gas from said separation zone, so as to maintain the latter under a high vacuum sufficient to suck the gas and the solid substance upwards through said delimited passage; in causing the solid substance to flow down towards the other of said contacting zones; adjusting the rate with which the solid substance is transferred from said pick-up zone to said separation zone, by adjusting the rate with which said second gas stream is introduced into said bed; and maintaining the total rate of gas flow in said bounded passage at a substantially constant value, compensating each adjustment of the rate in said second gas stream by an opposite and substantially equal rate adjustment in the said first stream of gas. 12 - Process for the cracking of hydrocarbons entering into the composition of petroleum; ,, consisting of: passing a granular contact substance up and down from a feed zone, in the form of a elongated and compact vertical current which moves by gravity towards a delimited transformation zone and against the pressure prevailing therein, while maintaining a gas sheet forming a seal near the lower end of said column of descent; passing the solid substance downwardly through said transformation zone in the form of a substantially compact column; in passing a fraction of the hydrocarbon in petroleum form in contact with said column at a suitable temperature to ensure the conversion by cracking of this hydrocarbon into a gasified product with a lower boiling point., and evacuating said gasiform product from said processing zone; passing the depleted contact substance downward from the bottom of said transformation zone, in the form of an unthrottled, gravitational downward compacta current to a delimited regeneration zone; passing the contact substance through said regeneration zone, in the form of a substantially compact column, while contacting it with a suitable regenerating gas, in order to regenerate it with a view to its re-use in said transformation zone; in passing the regenerated contact substance downwards, in the form of a compact and unthrottled current from the bottom of said regeneration zone to a substantially compact bed formed by said contact substance in a delimited lift system pick-up area; maintaining a delimited flow of lift gas directed upwardly from a point in said bed at a point intermediate at these ends to a point in said feed zone; maintaining communication between said elevating gas stream and said bed at a point below the surface of the latter and occupying a central position with respect to the horizontal section of said bed; passing a second stream of gas transversely through this bed and then notching said first stream, which has the effect of causing the contact substance to integrate with said first stream and to be raised by the mixed gas streams into said feed zone; to separate the gas from, then the 'contact substance contained in <Desc / Clms Page number 22> said supply zone and exhausting the gas separated from the upper part of this supply zone; to control the rate with which the contact substance flows downwards from said supply zone, through the transformation and regeneration zones, to the said bed contained in the said handling zone of the lifting system, by controlling only the flow. said second stream of gas; and maintaining the density of the contact substance in said bounded stream within limits of 3 to 24 pounds per cubic foot, by controlling the total flow rate with which the two gas streams are introduced. 130 A process for cracking hydrocarbons in petroleum form, comprising passing a granular contact substance downward from a feed zone in the form of a compact, vertical and elongated stream which flows by gravity to a delimited transformation zone and against the pressure prevailing therein, while maintaining a gas layer forming a seal near the lower end of said column; passing the solid substance downwardly through said transformation zone as a substantially compact column; in passing a fraction of the hydrocarbon consisting of petroleum in contact with said column and at a suitable temperature to ensure the transformation by cracking of this fraction into a gas-like product with a lower boiling point, and in removing said gas-like product of said transformation zone; passing the depleted contact substance down from the bottom of said transformation zone. - in the form of a compact current, not constricted and descending by gravity to a delimited regeneration zone; in passing the contact substance through said regeneration zone, in the form of a substantially compact column, while bringing it into contact with a suitable regenerating gas, in order to regenerate it with a view to its reuse in said transformation zone; passing the regenerated contact substance downwards ;, in the form of a substantially compact and un-throttled stream., from the bottom of said regeneration zone onto a substantially compact bed formed by said contact substance in one zone delimited support for the lifting system; maintaining a delimited elevation passage extending upwardly to said feed zone at a point below the surface of said bed but above the bottom thereof and occupying a central position by relative to the lateral dimensions of said bed, the lower end opening downwards, of this passage, being in communication with said bed; introducing a portion of a vapor stream into the lower end of said riser stream, into the interior of said bed, without forcing it to pass through any substantial portion of that bed; introducing the remaining portion of said vapor stream into said bed near the lateral periphery of the latter and causing it to pass transversely through this bed and then joining said delimited lifting stream, so as to bring the substance of contact to enter said boost current; controlling the rate with which the contact substance reaches said boosting current and, thereby, the rate with which the contact substance flows downward from the feed zone to the transformation and processing zones. regeneration, and therethrough to said bed contained in said elevation support zone, by adjusting the relative flow rates of said portions of the vapor stream, while maintaining substantially constant the total flow rate steam; separating the vapor from the contact substance contained in said feed zone and discharging the vapor from this zone to a barometric condenser, where this vapor is condensed, so as to maintain the zone feed under a vacuum sufficient to lift the contact substance with said boost current. 14. A continuous process for the transformation of hydrocarbons in the presence of a moving mass of granular contact substance, comprising passing a granular contact substance downwardly through a transformation zone. in the form of a substantially compact column., while bringing it into contact with fluid hydrocarbons, with a view to ensuring the transformation of said fluid hydrocarbons into gas-like products; removing said carbonated products from said conversion zone; to be evacuated separately <Desc / Clms Page number 23> Reacting the depleted contact substance from said transformation zone and passing it through a delimited revivification zone, passing said contact substance downwards, through said revivifying zone, in the form of a substantially compact column, while bringing it into contact with a regenerating gas to ensure the regeneration of said contact substance with a view to its re-use in said transformation zone; removing the revitalized contact substance from the lower part of said revitalizing zone;,. in the form of a substantially compact current descending by gravity; suspending said contact substance in a stream of carrier gas and sucking it upwardly through a limited and elongated passage into a separation zone situated above said transformation zone and kept under a notable void; ensuring separation of the contact substance from said carrier gas in said separation zone; sucking the separated carrier gas from said separation zone to maintain the latter under a substantial vacuum sufficient to ensure the elevation of said contact substance into said separation zone, as indicated above; inflowing the separated contact substance from the lower part of said separation zone downwardly in the form of a compact, elongated and substantially vertical feed column. \) of particles descending by gravity, into the upper part of said transformation zone; this feed column having a sufficient height for the contact substance to exert a pressure at least equal to the pressure difference between said transformation zone and said separation zone. 15. A continuous process for the transformation of hydrocarbons in the presence of a moving mass of granular contact substance, comprising: passing a granular contact substance downwardly through a transformation zone, in the form of a substantially compact column, while bringing it into contact with fluid hydrocarbons, to ensure the transformation of said fluid hydrocarbons into gas-like products, to evacuate said gas-like products from said transformation zone; separately removing spent contact substance from said transformation zone and passing it into a confined revivification zone; passing said contact substance downwardly through said revivification zone, in the form of a substantially compact column, while contacting it with a regenerator gas, to ensure regeneration of said contact substance with a view to its re-use in said processing zone; removing the revitalized contact substance from the lower part of said revivifying zone and securing its suspension in a stream of condensable transport gas., while practically preventing the introduction of a non-condensable gas into said stream. support gas stream; sucking the contact substance and the carrier gas upwardly through a delimited elevator passage to a delimited separation zone, maintained above said transformation zone; separating the carrier gas from the contact substance in said separation zone and passing it to a barometric condenser operating so as to condense said condensable carrier gas and maintaining said separation zone under sufficient vacuum to ensure elevation of the contact substance through said delimited elevation passage; in causing the separated contact substance to flow from the lower part of said separation zone downwards in the form of a compact, elongated and substantially vertical delimited feed column of particles descending by gravity, to in the upper part of said transformation zone, said feed column having a height sufficient for the contact substance to exert a pressure at least equal to the difference between the pressures of said conversion zone and of the known as the separation zone. 16 - Cyclic process for the conversion of hydrocarbons, consisting in passing a granular contact substance downwards through two separate and delimited contacting zones, arranged vertically in series one above the another one of these zones being a transformation zone and the other a revivification zone, to pass a load of hy- <Desc / Clms Page number 24> fluid hydrocarbon in contact with said contact substance in said transformation zone, to ensure the transformation of this hydrocarbon feedstock into a gas-like product; in evacuating said carbonated product from said transformation zone; passing a revitalizing gas in contact with said contact substance in said revitalizing zone; in causing the contact substance to flow from that of said contacting zones which is situated lowest downwards, starting from the latter zone ,. in the form of a stream substantially compacted to a point below said lowermost contacting zone and suspending this contact substance in a stream of carrier gas; in sucking this gas and the contact substance suspended therein upwards, as far as a separation zone situated above the highest of the contacting zones and maintained under a considerable vacuum; separating the carrier gas from the contact substance and sucking it from the upper part of said separation zone, so as to keep said zone under a sufficient vacuum to ensure the elevation of said substance contact in said separation zone, as indicated above; inflowing the separated contact substance, in the form of a compact column, descending by gravity, into the uppermost of said contacting zones; said column having a height such that the contact substance exerts at its lower end a pressure greater than the pressure difference between said separation zone and said highest contacting zone. 17 - Cyclic process for the conversion of hydrocarbons, consisting in passing a granular contact substance downwards through two delimited and separated contacting zones, arranged vertically one above the other, in series, one of these zones being a transformation zone and the other a revivification zone; in passing a charge constituted by fluid hydrocarbons in contact with said contact substance in said transformation zone, in order to effect the transformation of said hydrocarbon charge into a gas-like product; in evacuating said carbonated product from said processing zone; to pass a gas this EMI24.1 said revivification zone; passing the contact substance downwards from said lower contacting zone into a supply zone of the gas lift system; maintaining an atmosphere of a condensable gas in said feed zone of the elevator system; determining the suspension of said contact substance in a stream of condensable carrier gas in said feed zone of the elevator system and sucking the carrier gas and the contact substance suspended therein upwards. through a delimited passage, into a separation zone which is maintained under a sufficient vacuum to ensure the elevation of said contact substance through said passage and which is located at an appreciable distance above said zone of superior contacting; separating said carrier gas from the contact substance in said separation zone; passing the separated gas from said separation zone to a barometric condensation zone, where it is mixed with a cold liquid, so as to be condensed; controlling the operation in said condensation zone, so as to maintain said significant vacuum in said separation zone; inflowing the separated contact substance from the lower part of said separation zone in the form of a vertical column, essentially compact ,? granular substance descending by gravity, towards the highest of said contacting zones, the length of said column being sufficient to ensure the flow by gravity of said contact substance between said separation zone and said upper contacting zone. 18 - Process according to claim 17, characterized in that the said condensable carrier gas is steam. 19 - Cyclic process for converting hydrocarbons to lower boiling products, comprising passing a feed of liquid hydrocarbon into contact with a substantially compact column of granular contact substance running downward in a transformation zone delimited and maintained at a suitable temperature for the trans- <Desc / Clms Page number 25> forming said hydrocarbon feedstock into gas-like products with lower boiling points and at a pressure greater than atmospheric pressure; in removing said gas-like products from said processing zone; in passing the contact substance carrying a deposit of carbonaceous impurities from the lower part of said transformation zone, in at least one essentially compacted current towards a defined regeneration zone and kept at a short distance only below said transformation zone, and to maintain an anointed, inert gas along at least part of said stream at a point between them. known as conversion and regeneration zones; passing said contact substance downwardly through said regeneration zone, in contact with a gas containing oxygen, to ensure combustion of said deposit of impurities; to maintain'. in said regeneration zone, a pressure which is not appreciably greater than that prevailing in said transformation zone, so as to allow flow by gravity of the contact substance between said transformation zones and regeneration, through a flow column of short length; removing the regenerated contact substance from the lower part of said regeneration zone in the form of an essentially compact stream; and in introducing the regenerated contact substance, thus evacuated, into a stream of carrier gas which arises at a pressure close to atmospheric pressure, at the point of introduction of the contact substance; sucking the carrier gas and the contact substance upwards in the form of a stream delimited in a separation zone maintained under a substantial vacuum and situated at an appreciable distance above said transformation zone ; providing substantially complete separation of the carrier gas from the contact substance in said separation zone; in evacuating the separated gas from said separation zone, in order to maintain this zone under an appreciable vacuum; in causing the reghered contact substance to flow from the bottom of the latter zone downwards in the form of at least one compact, elongated and delimited column towards said transformation zone; said supply column having, above said transformation zone, a vertical height sufficient for, at its lower end, the contact substance to exert a pressure greater than the pressure difference between said transformation zones and of seperation. 20 - Cyclic process for the catalytic cracking of petroleum fractions, consisting of: passing a catalyst, granular downwards,? in the form of an essentially compact column, through a delimited transformation zone, maintained at a pressure higher than atmospheric pressure, while contacting it with a fluid fraction of petroleum and a suitable transformation temperature , in order to ensure the catalytic cracking of said fraction into a gas-like product with a lower boiling point; in discharging said carbonated product from said transformation zone; directing the spent catalyst downwardly carrying a carbonaceous deposit in the form of an essentially compacted stream from the bottom of said transformation zone to a regeneration zone situated a short distance below the first and only at a short distance above ground level; to maintain a vapor atmosphere under a pressure greater than that prevailing in the transformation zone, near the upper end of said compacta stream to pass said catalyst downwards through said regeneration zone, under the form of a substantially compact column, while bringing it into contact with a gas containing oxygen in order to burn said deposit; controlling the temperature of the catalyst in said regeneration zone, to keep it below the value corresponding to deterioration by heat; maintaining the pressure in said regeneration zone at a value lower than that of the pressure in said transformation zone, to allow flow by gravity of the catalyst from said transformation zone to said regeneration zone ,? in the form of a compact stream of short length; in discharging the regenerated catalyst from the bottom of the regeneration ditezone, in the form of an essentially compact stream of sufficient length and of sufficiently reduced cross section to prevent significant exhaust of. regenerator gas to said zone, together with the catalyst stream; in mixing said catalyst with <Desc / Clms Page number 26> a stream of vapor the pressure of which at the point where mixing takes place is not appreciably greater than atmospheric pressure; and drawing the stream of vapor and catalyst upwardly as a delimited and elongated stream to a separation zone maintained under a substantial vacuum; sufficient to ensure the elevation of the catalyst., this zone being situated at an appreciable vertical distance above said transformation zone; in separating the vapor from the catalyst in said separation zone - in sucking the vapor from said separation zone to a barometric condenser, in which this vapor is mixed with water and condensed, said condenser barometric operating so as to maintain said separation zone under appreciable vacuum; in passing the catalyst downwards, in the form of a delimited and substantially compact column, from said separation zone to said transformation zone, said column having a sufficient length to ensure the introduction of the catalyst in the transformation zone against the resistance opposed by the pressure prevailing therein; and maintaining an inert gas atmosphere near the lower end of said column, at a temperature higher than that prevailing in the transformation zone so as to prevent the escape of the reaction hydrocarbons to said separation zone. 21 - Cyclic process for the catalytic cracking of petroleum fractions consisting in passing a granular catalyst downwards, in the form of an essentially compact column; through a transformation zone delimited and maintained at a pressure greater than the atmospheric pressure while bringing this substance into contact with a fraction of liquid petroleum, at a suitable transformation temperature to effect the catalytic cracking of said 'fraction into' a lower boiling point gas-like product; in evacuating said carbonated product from said transformation zone; directing the spent catalyst carrying a carbonaceous deposit downwards, in the form of a substantially compact stream, from the bottom of said transformation zone to a regeneration zone situated a short distance below the zone transformation and at a short distance only above ground level; maintaining a vapor atmosphere at a pressure greater than that of the transformation zone near the upper end of said compact stream; passing said catalyst downwardly through said regeneration zone in the form of a substantially compact column while contacting it with an oxygen-containing gas to burn said deposit; controlling the temperature of the catalyst in said regeneration zone, to maintain it at a value lower than that corresponding to deterioration by heat; in maintaining the pressure in said regeneration zone below that which prevails in said transformation zone, so as to allow flow by gravity of the catalyst from said transformation zone to said regeneration zone, in the form of a compact stream of short length; discharging the regenerated catalyst from the bottom of said regeneration zone in the form of a substantially compact stream, of sufficient length and of sufficiently small section to prevent appreciable escape of regenerator gas from said zone, together with the catalyst stream; in introducing said catalyst into a delimited zone, maintained directly below the said regeneration zone; maintaining the last-mentioned zone at a pressure close to atmospheric pressure and under a vapor atmosphere, so as to essentially prevent any penetration of non-condensable gas into the latter zone; ensuring the suspension of said catalyst in a vapor stream in the last mentioned zone; drawing the stream of catalyst and vapor upwardly through a demarcated passage extending from bottom to top through the regeneration and transformation zones and terminating in an enlarged sedimentation zone situated at a height appreciable distance above the transformation zone and maintained under substantial vacuum sufficient to ensure catalyst elevation; to ensure the separation of the catalyst and the steam in said sedimentation zone; in evacuating the vapor from the upper part of said sedimentation zone to a barometric condenser operating in such a way as to condense said vapor and creating a suction maintaining the appreciable vacuum in said sedimentation zone; <Desc / Clms Page number 27> in passing the separated catalyst from the bottom of said sedimentation zone, in the form of a substantially compact column and descending by gravity, towards said transformation zone, this column having a sufficient height so that the catalyst exerts at its lower end a pressure greater than the difference between the pressures of said sedimentation zone and of said transformation zone; and maintaining a sheet of inert gas near the lower end of said column at a pressure greater than that of the transformation zone situated immediately below. so as to prevent the escape of hydrocarbon from said transformation zone towards said sedimentation zone. 22 - Cyclic process, for the transformation of hydrocarbons, consisting in passing a granular contact substance downwards through two contact zones delimited and separated and situated vertically one above the other in series, \) one of said zones being a transformation zone and the other being a revivification zone; passing a charge of fluid hydrocarbons in contact with said contact substance in said processing zone to effect the transformation of said charge of hydrocarbons into a gas-like product; removing said carbonated product from said processing zone; passing a revitalizing gas in contact with said contact substance in said revitalizing zone; passing the contact substance downwardly from said lower contacting area to a supply area of the gas lift system; maintaining a condensable gas atmosphere in said feed zone of the elevator system; suspending said contact substance in a condensable carrier gas stream in said feed zone of the elevator system; and sucking up the carrier gas and the contact material suspended therein through a delimited passage, to a separation zone maintained under a sufficient vacuum to ensure the elevation of said contact material through. said passage and which is located a substantial distance above said upper contact zone; separating said carrier gas from the contact substance in said separation zone; passing the separated gas from said separation zone to a barometric condensation zone, in which it is mixed with a cooling liquid, to be condensed thereby producing a vacuum in said separation zone; controlling the value of the vacuum in said separation zone by introducing a non-condensable gas into said barometric condensation zone, with a controlled flow rate; sucking the non-condensing gas from the upper part of said barometric condensation zone; inflowing the contact substance thus separated from the lower part of said separation zone in the form of a substantially compact vertical column of granular substance descending by gravity to the uppermost of said contacting zones; the length of said column being sufficient to ensure displacement by gravity of said contact substance between said repair zone and said upper zone of the contact. 23 - In a continuous process for the conversion of hydrocarbons, in which a granular contact substance is caused to pass in a cyclic fashion through two contacting zones, one of these being a conversion zone where this substance is brought into contact with a charge of fluid hydrocarbons in order to effect the transformation of these into the desired gasiform products, the other zone being a regeneration zone, where this substance is placed. in contact with an appropriate regeneration fluid, to be regenerated with a view to its reuse in the said transformation zone: the improved method for transferring the contact substance from one of these contacting zones to the other and consisting : causing the contact substance to flow downwardly from said contacting zones, in the form of a substantially compact stream, to a point below this zone and where this substance is integrates at a suspension current of one. suitable lift gas; sucking the lift gas and the contact substance suspended therein upwardly in the form of a delimited stream, into a separation zone situated above the other contacting zone; separating the contact substance from the lifting gas and sucking this gas <Desc / Clms Page number 28> from said separation zone, so as to maintain this latter zone: under a sufficient vacuum to ensure the elevation of the contact substancea as indicated above and to cause the separated contact substance to flow from said separation zone downwards and by gravity to the other contacting zone . 24 - In a continuous process for the transformation of hydrocarbons, in which a granular contact substance is caused to pass in a cyclic fashion through two contacting zones, one of these being a transformation zone, in which -this substance is brought into contact with a charge of fluid hydrocarbons, to effect the transformation of this substance into the desired gasiform products, while the other zone is a regeneration zone, in which this substance is brought into contact with Suitable regeneration fluid, to be regenerated for re-use in said transformation zone - the improved method of transferring contact substance from one of said contacting zones to another, consisting of: causing the contact substance to flow downwardly from one of said contacting zones, in the form of a substantially compact stream, to a supply zone of the gas lift system. located below said contacting zone, - ensuring the suspension of said contact substance in a condensable lifting gas stream, in said supply zone of the lifting system; and conveying the contact substance suspended upwardly in said stream, to a delimited separation zone, located above the other of said contacting zones and maintained under a vacuum sufficient to sucking the contact substance and the lift gas upwards from said supply zone; separating the lift gas from the contact substance and passing the lift gas to a barometric condensation zone, in which this gas is mixed with a cold liquid so as to condense the lift gas and thereby cause said vacuum to act in said separation zone; and inflowing the separated contact substance from said separation zone to said other of said contacting zones in the form of a substantially compact stream flowing by gravity, 25 - Cyclic process for the conversion of hydrocarbons, consisting of: passing a granular contact substance downwards through two separate and delimited contacting zones, arranged vertically one above on the other in series, one of said zones being a transformation zone and the other being a regeneration zone; passing a charge of fluid hydrocarbons in contact with said contact substance in the transformation zone, to effect the transformation of said charge into a gas-like product; in evacuating said carbonated product from said transformation zone; in passing a regenerating gas in contact with the contact substance in said regeneration zone, in order to effect the regeneration of the contact substance with a view to its reuse in said transformation zone; in causing the contact substance to flow downwards, in the form of a direct current, essentially compact and not constricted, from those, of the two said contacting zones which is situated lower, to a substantially compact bed of contact substance, kept in a separate zone, below, from the latter zone, so as to constantly ensure the compactness of the current of contact substance rising from said bed and heading towards the two placing zones in contact with and through them; maintaining a vapor atmosphere at least in the lower part of said bed; and causing the contact substance contained in said lower part of said lite to integrate with an ascending vapor stream by which this substance is raised through a delimited passage, towards a separation zone located above the zone upper contacting; separating the vapor from the contact substance in said separation zone and sucking the separated vapor from the upper part of said zone to a barometric condensation zone, where this substance is contacted with water, to ensure its condensation, said vapor being sucked from said separation zone with a sufficient flow rate to maintain a substantial vacuum therein, which ensures the elevation <Desc / Clms Page number 29> of the contact substance up to said separation zone, as described above; allowing steam to enter the lower end of said stream, to replace that which has been drawn in from said separation zone; passing the contact substance downwardly from the lower part of said separation zone, as a vertical and substantially compact stream, to the upper contacting zone, said compact stream having a vertical height sufficient to ensure gravity lifting of the contact substance to the upper contacting zone against the resistance of the pressure exerted therein; and controlling the rate of circulation of the contact substance through said system, by simply adjusting the flow rate of the contact substance from the space above the surface of said bed into said gas stream support. 26. Cyclic process for the transformation of hydrocarbons into products with a lower boiling point, consisting in passing a contact substance: granular downwards through two contacting zones arranged vertically in series, in which zones the contact substance flows in the form of a substantially compact column, and between which the zones this substance flows as a delimited and unstrangled compacted stream, of relatively small cross section, 9 one of said zones the contact being a reaction zone and the other being a regeneration zone; passing fluid reaction hydrocarbons in contact with the contact substance in said reaction zone at a pressure greater than atmospheric pressure and at a temperature suitable for ensuring the conversion of said reaction hydrocarbons into gas-like products at higher low boiling point; sucking said products from said reaction zone; maintaining an inert gas seal near the upper and lower ends of said reaction zone, to prevent escape of the reaction hydrocarbons through the inlet and outlet streams of the contact substance to pass a gas suitable regenerator in contact with the contact substance in said regeneration zone, at a pressure above atmospheric pressure and at a suitable temperature to ensure the regeneration of the contact substance with a view to its re-use in said reaction zone; passing the contact substance from that of said contacting zones which is situated lowest, in the form of a substantially compact and unthrottled stream, to a decompression zone, where the current is communication with the atmosphere; in causing the contact substance to flow from said decompression zone, in the form of an unthrottled compacta current descending by gravity, onto the surface of a substantially compact bed of said contact substance contained in a delimited zone power supply to the lifting system; causing the contact substance located at a point in said bed which is below the surface and above the bottom thereof to become part of an elevating vapor stream; andspiring the uplift vapor and the contact substance upwardly as a bounded stream, to a sedimentation zone located above the upper contacting zone and maintained under a substantial vacuum, which is sufficient to provide the lift, to separate the lift vapor from the contact substance. in said sedimentation zone; and sucking this vapor to a barometric condensing zone operating to condense the vapor and maintain a vacuum in said settling zone; .allowing the entry of replacement vapor into the lower end said rise current; inflowing the contact substance from said settling zone, in the form of a compact, unthrottled, gravity-moving feed column to the upper contacting zone against the resistance of the pressure exerted in it; and controlling the flow rate of the descending current of contact substance from said settling zone to and through the contacting zones, and further down to said bed in said zone of contact. feeding of the elevator system, by adjusting the rate with which the contact substance is introduced, from inside said contained beds, into said supply zone of the elevator system, into said elevating vapor stream ,. ., <Desc / Clms Page number 30> 27. Apparatus for the continuous transformation of hydrocarbons in the presence of a granular contact substance moving cyclically, this apparatus comprising in combination: two contacting chambers placed one above IL-the other., each of these chambers comprising separate gas inlets, as well as separate gas outlets, remote from these inlets, these chambers further comprising inlets for the solid substance at their upper ends and outlets for the solid substance at their lower ends; a vertical and unthrottled conduit for the flow of the solid substance, connecting the solid substance outlet of the upper chamber to the solid substance inlet of the lower chamber; a separation chamber located a substantial distance above the upper contacting chamber; a vertical feed duct connecting the upper part of the separation chamber to the solid substance inlet of the upper contacting chamber; a gas outlet duct leading to the separation chamber near the upper end thereof; a vessel called to delimit a bed of contact substance located below the lower contacting chamber; elements delimiting an unthrottled passage, extending downwards, for the flow of the solid substance from the lower part of:; the lower contacting chamber to the upper part of said vessel; elevation duct extending upwards from a point situated in the lower part of said vessel, but above the bottom thereof, to a point situated in the interior of said separation chamber, intermediate at the upper and lower ends thereof, said duct being open at its upper end and having a flared open lower end; a cylindrical gas inlet member fixed to the bottom of said vessel and extending upwardly to a level near the flared lower end of said elevation duct; a conically shaped cap on said gas inlet member, extending upwardly into the interior of said flared lower end of said elevation duct; said conical cap having lateral dimensions smaller than those of said flared lower end of the lifting duct, so as to leave an annular passage for the entry of gas and contact substance between the conical cap and said lower flared end of said riser duct; openings in said conical cap, to allow passage of gas from the interior of the inlet member to said riser gas duct; an exterior gas inlet pipe; a constant flow control device on this duct; a three-way valve on this pipe upstream of said flow control device; a tube connected between said three-way valve and said cylindrical gas inlet member; a gas distribution element extending around the internal side wall of said vessel, at a level intermediate the ends thereof; a tube connecting said distribution element and said three-way valve; a flow control valve on said last named tube. 28. Apparatus for the continuous transformation of hydrocarbons in the presence of a cyclically moving contact substance, comprising in combination: two contacting chambers arranged one above the other. on the other, these chambers each comprising separate gas inlets as well as separate gas outlets distant from said inlets, as well as solid substance inlets at their upper ends and solid substance outlets at their lower ends; a vertical, un-throttled conduit for the flow of the solid substance, connecting the solid substance outlet of the upper chamber to the solid substance inlet of the lower chamber; a separation chamber located a substantial distance above the upper contacting chamber; a vertical feed duct connecting the lower part of the separation chamber to the solid substance inlet of the upper contacting chamber; a gas outlet duct terminating in the separation chamber near the upper end thereof; a vessel called to delimit a bed of contact substance, located below the lower contacting chamber; elements defining a non-constricted passage extending downwards, for the flow of the solid substance from the bottom of the contacting chamber <Desc / Clms Page number 31> lower towards the upper part of said vessel, an elevation duct extending upward from a point in the interior of the lower part of said maize vessel above the bottom thereof. here, up to a point located inside said separation chamber, intermediate at the upper end and at the bottom thereof, said duct being open at its upper end and being at least partially open to its lower end; means delimiting a passage, for the introduction of a gas ,. in the lower end of said elevation duct, from a point outside of said vessel; a pipe for the introduction of gas into the lower part of said vessel at a point remote from the open lower end of said elevation pipe. 29., Apparatus for the continuous transformation of hydrocarbons in the presence of a granular contact substance moving in a cyclic manner, comprising in combination two contacting chambers located one above the other , each of these chambers comprising separate gas inlets and separate gas outlets, spaced from said inlets, these chambers further comprising split substance inlets at their upper ends and solid substance inlets at their ends lower; an unthrottled vertical pipe. for the flow of the solid substance., connecting the solid substance outlet of the upper chamber to the solid substance inlet of the lower chamber; a separation chamber located at a substantial distance above the upper contacting chamber; a vertical supply line connecting the lower part of the separation chamber to the solid substance inlet of the upper contacting chamber; a barometric condenser; a duct connecting the upper part of said separation chamber to said barometric condenser; an elevator system feed tank, located below the lower contacting chamber; means determining a downwardly extending and unconstrained passage for the flow of the contact substance from the bottom of the lower contacting chamber to a point near the upper end of said supply tank; an elevation duct extending upwards from its open lower end and opening downwards, the end located at a central point inside the lower part of said supply tank, above the bottom of the tank. the latter, up to a point inside said separation chamber, between the ends of said separation chamber; elements determining a passage for the admission of gas into the lower end of said riser duct; a conduit for the admission of gas, terminating at the side wall of said supply tank; in the lower part of it; a flow restriction device attached to the duct named last. 30. Apparatus for the continuous transformation of hydrocarbons in the presence of a granular contact substance moving in a cyclic manner, comprising in combination: two contacting chambers located one above the antrum. ; each of said chambers comprising separate gas inlets and separate gas outlets, spaced from these inlets, these chambers further comprising solid substance inlets at their upper ends and solid substance outlets at their lower ends ; a vertical, unthrottled, conduit for the flow of the solid substance, connecting the solid substance outlet of the upper chamber to the solid substance inlet of the lower chamber, a separation chamber located at a distance appreciable above the upper contacting chamber; a vertical supply line, connecting the lower part of the separation chamber to the solid substance inlet of the upper contacting chamber; a gas outlet pipe terminating in the separation chamber, near the upper end thereof; a vessel called to delimit a bed of contact substance placed below the lower contact chamber; members defining an unthrottled, downwardly extending passage for the flow of the solid substance from the bottom of the lower contacting chamber to the upper part of said vessel; an elevation duct extending upwards from a point: located in the interior of the lower part of said va'se, but 'above the bottom thereof!) to a point located in the interior of said separation chamber, inter- <Desc / Clms Page number 32> medially at the upper and lower ends thereof; said duct being open at its upper end and being at least partially open at its lower end; an outlet for gas, terminating at said vessel directly below the lower end of said riser duct; a gas inlet duct arranged externally; a three-way valve provided on said inlet duct; a pipe connecting said gas inlet to said valve; at least one inlet tube of. gas emerging in the side wall of said vessel, at a level close to that of the lower end of said elevation duct; a line connecting said last-mentioned gas inlet to said three-way valve; and a constant flow adjustment device provided on said gas inlet pipe upstream of said three-way valve. 31 - Improved apparatus for the pneumatic transport of granular contact substance, comprising: a supply chamber called to delimit a bed of contact substance, passage means for bringing the contact substance into the upper part of said contact substance. feeding chamber; a receiving chamber located at a higher level than said supply chamber; a riser tube extending upwardly to said receiving chamber, from a point in said silencing chamber below the passage means for the arrival of the contact substance, but at above the bottom of said feed chamber; said riser tube having an open, flared lower end opening downwards; a gas inlet duct opening into said supply chamber and terminating directly below said flared and open end of said riser tube; a perforated, vertical and conical dispensing head provided on the end of said inlet duct; said head having a perforated area for the passage of gas which is not substantially less than the horizontal free section of said riser tube above the level of its flared lower end; and a second gas inlet opening into said supply chamber at a point separated by an appreciable distance from the lower end of said riser tube and situated a small distance below the level of this end. 32.- Apparatus for the continuous transformation of hydrocarbons in the presence of a granular contact substance moving in a cyclic manner; comprising: a transformation chamber having a solid substance inlet at its upper end and a solid substance outlet at its lower end; means for introducing fluid hydrocarbons into said chamber and -means for discharging gas-like products therefrom; a regeneration chamber located below said transformation chamber; a solid substance inlet at the upper end of said regeneration chamber and a solid substance outlet at the lower end thereof; a short conduit, substantially vertical, connecting the solid substance outlet of said transformation chamber to said solid substance inlet of said regeneration chamber; means for maintaining an inert gas atmosphere in the transformation chamber immediately above said duct; means for admitting gas into said regeneration chamber and means for discharging gas from: this chamber; a settling chamber located a substantial distance above said transformation chamber; a vertical riser duct extending upwardly from a point below said regeneration chamber to a point within the interior of said settling chamber; means delimiting a passage for the flow of solid substance from the lower part of said regeneration chamber to a point near the lower end of said lifting duct; a pipe for the admission of steam into the lower end of said lifting duct; a barometric condenser; means for supplying water to said condenser; a pipe connecting said condenser to the upper part of said sedimentation chamber; elongated vertical duct, connecting the lower part of said sedimentation chamber to the upper part of said transformation chamber; and means for maintaining an inert gas atmosphere near the lower end of said duct. <Desc / Clms Page number 33> 33. Apparatus for the continuous transformation of hydrocarbons in the presence of a granular contact substance moving in a cyclic manner, comprising: a transformation chamber having a solid substance inlet at its upper end and an outlet of solid substance at its lower end; means for introducing fluid hydrocarbons into said chamber and means for discharging gasiform products therefrom; a duct extending vertically through said transformation chamber, fitted tightly to its upper end open in the upper wall of said chamber - and hermetically fitted to its lower end open in the bottom wall of said chamber, so as to constitute a hollow column passing through said chamber and open at its ends, but not in communication with the interior of said transformation chamber; a regeneration chamber located below said transformation chamber; a solid substance inlet at the upper end of said regeneration chamber and a solid substance outlet at the lower end thereof; short, substantially vertical conduit connecting the solids outlet of said transformation chamber to said solids inlet of said regeneration chamber; means for maintaining an inert gas atmosphere in the transformation chamber immediately above said conduit; means for introducing gas into said regeneration chamber and means for discharging gas from this chamber; a vertical duct extending through said regeneration chamber and the open upper end of which fits tightly into the upper wall of said regeneration chamber, while its open lower end is hermetically fitted into the bottom wall of this chamber, so as to constitute a hollow and open vertical column ;, passing through said regeneration chamber; the last named hollow column being vertically aligned with the hollow column passing through said transformation chamber; a mixing chamber located a short distance below said regeneration chamber; and a closed settling chamber located a substantial vertical distance above said transformation chamber; means determining a passage for the flow of solid substance from the solid substance outlet of said regeneration chamber to said mixing chamber; a vertical riser duct extending upwardly from the interior of said mixing chamber to said hollow columns and extending freely therethrough, passing through the regeneration and transformation chambers and terminating by its upper end in said sedimentation chamber; a gas evacuation device; and a pipe connecting said gas evacuation device to the upper part of said sedimentation chamber; means for admitting gas to the lower end of said elevation duct; an elongated vertical duct, connecting the lower part of said settling chamber to the upper part of said transformation chamber; and means for maintaining an atmosphere of inert gas near the lower end of said conduit. Apparatus for the continuous transformation of hydrocarbons in the presence of a granular contact substance moving in a cyclic manner, comprising a transformation chamber having a solid substance inlet at its upper end and a solid substance outlet at its upper end. its lower extremity; means for introducing fluid hydrocarbons into said chamber; and means for evacuating gasiform products from this chamber '; a duct extending vertically through said transformation chamber hermetically fitted at its upper end open in the upper wall of this chamber and hermetically fitted at its lower end open in the bottom wall of said chamber, so as to constitute a hollow column passing through said chamber and open at its ends, but not communicating with the interior of said transformation chamber; a regeneration chamber located below said transformation chamber; a solid substance inlet at the upper end of said regeneration chamber and a solid substance outlet at the lower end thereof; a short, substantially vertical duct connecting the substance outlet. solid from said transformation chamber to said solid substance inlet <Desc / Clms Page number 34> of said regeneration chamber? means for maintaining an inert gas atmosphere in the transformation chamber immediately above said duct; means for admitting gas into said regeneration chamber and means for discharging gas from this chamber; a vertical duct extending through said regeneration chamber and of which the open upper end is; hermetically fitted in the upper wall of said regeneration chamber, while its open lower end is hermetically fitted in the bottom wall of this chamber, so as to constitute an open vertical column passing through said regeneration chamber; said last named hollow column being vertically aligned with the hollow column passing through said transformation chamber; a closed sedimentation chamber located an appreciable vertical distance above said transformation chamber; a vertical riser duct extending upwardly from a location below said regeneration chamber, through hollow columns provided in said regeneration and transformation chambers, and terminating therein said sedimentation chamber ;. an outlet duct connected to said solid substance outlet provided at the lower end of said regeneration chamber; means for introducing the contact substance from said outlet duct into said elevation duct, near the lower end thereof; a barometric condenser; means for supplying water to said condenser; a pipe connecting said condenser to the upper part of said sedimentation chamber; an elongated vertical duct connecting the lower part of said sedimentation chamber to the upper part of said transformation chamber; and means for maintaining an inert gas atmosphere near the lower end of said conduit. 35.- Apparatus for the continuous transformation of hydrocarbons comprising in combination: two contacting chambers close to each other and situated one above the other; the bottom of the lower chamber being only a short distance above the ground; said chambers comprising separate gas inlet means and separate gas outlet means, these chambers further comprising solid substance inlets at their upper ends and solid substance outlets at their lower ends; a short vertical duct connecting the solid substance outlet of the upper vessel to the solid substance inlet of the lower vessel; means for introducing an inert gas forming a seal into said duct; a conduit. extending vertically through the upper chamber, the open top end of which fits tightly into the upper wall of the said upper chamber and the open lower end of which fits tightly into the bottom wall of the chamber. said upper chamber, so as to form a vertical hollow column passing through the upper chamber, and open at its ends, but not communicating with the interior of this upper chamber; a vertical duct extending in the same way through the lower chamber, to form a similar vertical hollow column passing through the latter chamber and vertically aligned with the hollow column passing through the upper chamber; a sedimentation chamber placed at an appreciable vertical distance above said upper chamber; a vertical riser pipe extending upwards from a location below the lower chamber, crossing said vertical hollow columns and terminating at its upper end in the interior of said settling chamber ; means for admitting an elevating gas to the lower end of said elevating duct; means for passing solid substance from the bottom of said lower chamber to a point of said elevation duct, located near the lower end thereof; means for evacuating lift gas from the upper part of said settling chamber; a vertical duct extending downward from the bottom of said elevation chamber to the top of said transformation chamber; and means for introducing an inert gas into the lower end of the last named conduit. 36 - Apparatus for the continuous transformation of hydrocarbons, comprising, in combination,: two contacting chambers located one on the other. <Desc / Clms Page number 35> above the other, each of these chambers having separate gas inlets and separate gas outlets, spaced from said inlets, and also having solid substance inlets at their upper ends and solid substance outlets at their upper ends. their lower extremities; an unthrottled vertical conduit for the flow of the solid substance, connecting the solid substance outlet of the upper chamber to the solid substance inlet of the lower chamber; a closed feed hopper, placed at an appreciable distance above the upper contacting chamber; a vertical tube connecting the lower part of said hopper to the solid substance inlet of the upper contacting chamber; a barometric condenser comprising a water inlet and a barometric duct; a duct connecting the upper part of said feed hopper to said barometric condenser; means for venting gas from the top of said barometric condenser; a separate gas inlet to said barometric condenser; a flow control valve provided on said inlet; a control device called to control the opening of said valve under the influence of changes in the pressure in said feed hopper; a riser tube extending upwardly from a location below; the lower contacting chamber to a point in the interior of said feed hopper, intermediate at the ends thereof. interior of said feed hopper, intermediately at the ends thereof; means for passing the solid substance from the bottom of said lower contacting chamber to the lower end of said riser tube; means for admitting steam at the lower end of said riser tube.