JPS6026439B2 - Hydrocarbon feed liquid distribution method and its equipment - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION The technical field to which the present invention pertains is the treatment of hydrocarbons using fluidized bed catalysts.

More particularly, the present invention relates in one aspect to a hydrocarbon donor liquid distributor and in another aspect to a method for injecting hydrocarbon donor liquid into a catalytic conversion zone. Both are particularly useful in fluidized catalyst cracking processes. A fluid catalytic cracking (FCC) pump to which the present invention can be applied particularly advantageously. Seth ``mixes a hydrocarbon feed stream with a boiling point range of about 260 to 0 in a riser reaction zone with a catalyst capable of fluidizing the hydrocarbon feed stream, where under conversion conditions the hydrocarbon feed stream is Generally, the temperature of the hydrocarbon donor stream is about 177-371°C and the temperature of the regenerated catalyst is about 621-7320°C. , the hydrocarbon-feeding stream is completely vaporized, and the temperature in the conversion zone is approximately 4 to
It becomes 593qC. Other typical conversion conditions include pressures from about atmospheric to about 7. *Atmospheric pressure is low, and hydrocarbon residence time is approximately 0.5 seconds to 5 minutes. Catalyst is typically circulated through the riser reaction zone at an amount of about 1.8 to 9.1 k9 catalyst per pound of hydrocarbon. The catalytic reaction may be carried out completely in the riser reaction zone, as in a full riser FCC unit, or it may be carried out only partially in the riser reaction zone, where the catalyst, reaction products, and unconverted feed (if present) are The mixture consisting of is then sent to a dense catalyst fluidized bed,
There are also methods for further converting pickles, or for converting expensive reaction products into more expensive reaction products.
The apparatus and method of the present invention is useful in both cases. Various methods have been used in the past to introduce hydrocarbon feed streams into riser reaction zones. For example, U.S. Pat. No. 3,152,065 describes a method for injecting a hydrocarbon feedstock into a catalytic reaction zone by flowing liquid hydrocarbons in a generally linear direction as an outer stream and imparting a centrifugal energy component to the outer stream. discharging the mobile hydrocarbon stream from a constricted channel in contact with an inner stream of vaporous material, such as water vapor, which serves to disperse the hydrocarbon stream into small droplets; A method consisting of the following is described. Other vaporous or gaseous materials can also be used as the inner stream, such as inert gas nitrogen, natural gas, and recirculating cracker process gas. The patent also discloses a nozzle for injecting liquid hydrocarbons into contact with a catalyst that includes an element for imparting a centrifugal energy component to the material flowing through the nozzle barrel. Both the method and the nozzle are intended to provide a high degree of atomization of the feedstock and sufficient contact of the hydrocarbon feedstock with the catalyst. This high degree of fogging is achieved by employing means of imparting a centrifugal energy component to the liquid hydrocarbon stream and by the use of "vaporous substances" which act to disperse the hydrocarbon stream into small droplets.
U.S. Pat. No. 36,140 discloses directing a substantially liquid hydrocarbon oil feedstock to at least one feed injection zone of a fluidized bed catalytic cracking reaction zone and simultaneously injecting water vapor/liquid into the injection zone. Hydrocarbon volume ratio is approximately 3-7
5, and the bagging speed of the resulting mixture relative to the fluidizing catalyst is at least about 30.5 skins/s.
An improved catalytic cracking process is described that consists of essentially complete atomization of a feedstock hydrocarbon oil into droplets with a diameter of about 350 r or less, such that ec.

The method includes the use of water vapor and at least 30.5 kites/sec to achieve high V feedstock atomization characterized by droplet sizes of about 350 mm or less in diameter.
This method relies on extremely high bagging speed. Conventional methods and apparatus, such as those described above, focus on initial catalysis of the hydrocarbon feed and catalyst to obtain, at least initially, a homogeneous mixture of catalyst and hydrocarbon feed within the riser reaction zone. , thereby preventing excessive coking of the V feedstock and associated product losses.

While it is certainly important to initially form a homogeneous mixture of catalyst and hydrocarbon, it is equally important that the homogeneity of the mixture is maintained as much as possible over the entire length and cross-section of the riser reaction zone. It is. More specifically, despite the use of methods and equipment to achieve initial homogeneous catalysis of hydrocarbon feed confluence and cracking catalyst, the cross-section of a typical riser reaction zone, particularly in the cross-sectional direction of its lower part, It was found that wide variations in sheer density and temperature may exist. Using a transducer equipped with a neck radiator and a thermocouple, the catalyst density and temperature in the riser reaction zone were measured at various heights;
The distribution map of catalyst density and temperature was obtained. In one section toward the bottom of the riser reaction zone, the catalyst density was found to be about 961 kg/m near the outer wall, compared to about 48 kg/m near the centerline of the riser. The temperature distribution also showed similar large fluctuations. In the lower cross-section of the standpipe reaction zone, high temperatures of over M9:00 were measured near the drop, but the temperature near the riser's centerline was approximately 0.
Met. Such high wall temperatures cause elongation of the riser reaction zone, often exceeding the designed wall temperature, resulting in permanent deformation of the riser reaction zone. Another effect of high wall temperatures is to cause overcracking of the hydrocarbon feedstock in this high temperature region, increasing the positive formation of dry gas (C2-). The apparatus and method of the present invention eliminates these high wall temperatures and the problems associated therewith. The apparatus and method provide a flatter cross-sectional temperature distribution in the riser reaction zone, thereby reducing overcracking and reducing the risk of damage to the riser reaction zone. It is therefore an object of the present invention to provide an improved fluidized bed catalytic cracking process that overcomes the conventional deficiencies mentioned above.

Another object of the present invention is to reduce the wall temperature of the reactor tube and to reduce the wall temperature of the reactor tube as a hydrocarbon feed distributor used to contact a hydrocarbon feed bulk stream with a fluidizable catalyst in a riser reactor tube. It is an object of the present invention to provide a distributor that can further reduce overcracking and the amount of dry gas produced.

Yet another object of the present invention is a method for injecting hydrocarbon-providing groove fluid into a riser reaction zone into contact with a fluidizable catalyst, thereby reducing the wall temperature of the zone. The object of the present invention is to provide a method in which overcracking and dry gas production are reduced.

In summary, the present invention provides, in one aspect, a conical combination having a small diameter end and a large diameter end connected to a hydrocarbon feed inlet; a circular plate attached to said main diameter machine having a hole and a plurality of second through holes: {c' attached to said first through hole and adapted to guide the first inlet and the hydrocarbon feed into the center; one or more first nozzles having a discharge outlet disposed; and {d) attached to the second through hole to direct the second inlet and the hydrocarbon feed downstream to the inner wall. a plurality of second nozzles having second discharge ports arranged to collide; , and a regenerated catalyst inlet, the regenerated catalyst inlet passing through each wall at a location downstream from the hydrocarbon feed inlet, the conversion conditions A hydrocarbon feed channel liquid distributor injects and contacts the hydrocarbon feed to the fluidized catalyst below.

In another aspect, the invention provides a method for delivering a first portion of a hydrocarbon feed to one or more first nozzles having an 'a' first inlet and a first outlet, and bringing the first nozzles into contact. vertically disposed in a conversion zone, thereby vertically guiding a first portion of the hydrocarbon feed from the first outlet to a central portion of the catalytic conversion zone;'b ' has a second inlet and a second outlet; the center line passing through the long axis of the second nozzle is angled toward the inner wall of the catalytic conversion reaction zone from the vertical center line passing through the center of the second inlet; A second portion of the hydrocarbon feed is delivered to a plurality of second/spools arranged in the side conversion zone in a diagonal manner, and the second portion of the hydrocarbon feed is and c- causing the hydrocarbon feedstock from the first and second nozzles to exit a second outlet and impinge on a downstream inner wall of the second outlet under conversion conditions. A method of distributing a hydrocarbon feed liquid by injecting a hydrocarbon feed material into contact with a fluidized catalyst in a catalytic conversion zone having a center and an indentation.

Other aspects and objects of the invention include details such as the function and arrangement of the various components of the inventive bag and the operating conditions of the inventive method, all of which are discussed below. Disclosed in the more detailed description. The bag hawk and method of the present invention have been briefly described above, and the present invention will now be described in more detail with reference to the accompanying drawings.

Although the drawings illustrate preferred embodiments of the present invention, the present invention is not limited to these embodiments, and all modifications, corrections, and equivalents included within the scope of the present invention. It is understood that it includes such things as It will also be appreciated that the drawings show only those details necessary for an understanding of the invention, and other details have been omitted for the sake of clarity. The invention is most advantageously utilized, particularly in a fluid catalytic cracking apparatus such as that shown in FIG.

The diamonds shown in Figure 1 include a riser reactor conduit 1, a feed liquid distributor 2, a hydrocarbon inlet 3, a regenerated catalyst inlet 4, a receiver tank 6, a cyclone separation bag 12, and a spent catalyst outlet. It consists of 16 pieces. A hydrocarbon feedstock, for example a virgin gas oil having a boiling point in the range of about 3 to 0, is introduced into the apparatus through a hydrocarbon feed inlet 3. This hydrocarbon feed may be preheated by a direct-fired heater (not shown) or a heat exchanger (not shown) prior to entering the unit, and the recycle stream may be combined with the virgin feed. It can be seen that it may be supplied to the device. The hydrocarbon complex may be in the gas phase, liquid phase, or a mixture thereof, but in the case of fluid catalytic cracking processes, it is more typically in the liquid phase. The hydrocarbon feed 9 channel inlet 3 is connected to a hydrocarbon liquid distributor 2 through which the hydrocarbon feed is mixed with the hot regenerated catalyst in the lower part of the riser reactor conduit 1. The regenerated catalyst is from a regeneration zone (not shown) and is passed through a regenerated catalyst inlet 4 provided with flow control means 5 for controlling the flow of regenerated catalyst to the riser reactor conduit 1 (simply referred to as (referred to as conduit 1). Essentially complete vaporization of the hydrocarbon feedstock occurs rapidly, and under conversion conditions such as the presence of regenerated catalyst, conversion of the feedstock occurs as the mixture flows upwardly within conduit 1. .
A conduit 1 extends upwardly from the bottom of the receiving tank 6 to a separation space 8 within it, the reaction products and the conversion feed, if present, being carried from the entrance 7 located at the upper end of the conduit 1 to this conduit. 1 and enters the separation space 8 in the receiving tank 6. Some separation of hydrocarbon vapor and catalyst also occurs in this separation space. This is because there is an increase in the velocity of the steam-catalyst mixture and a change in flow direction. The separated spent catalyst flows into a dense bed (deme d) 10 having an interface 9, hydrocarbon vapors and inert substances in the separation space 8 and the entrained catalyst are transferred from the inlet 11 to the cyclone separator 2.
The catalyst and steam are separated again, and the separated catalyst is sent down the dense bed 1 through the bevel leg 13, and the steam is passed through the steam conduit 17 to the cyclone separator. 12 and from the receiving tank 6. Although FIG. 1 shows only one cyclone separator 12, two or more such devices may of course be used in parallel or series flow relationship depending on the volume of steam flow, the load, and the degree of separation required. You can also use The catalyst in the dense bed 10 flows downwardly, through the lower neck-down portion of the receiver 6 and over the baffle 14 . This further displaces the adsorbed hydrocarbons and the interstitial hydrocarbons by a cocurrent flow of a stripping medium, generally water vapor. This stripping medium enters the lower part of the consignment 6 through its inlet 15. The spent catalyst passes through a spent catalyst conduit 16 to a receiving tank 6.
and is sent to a regenerator (not shown) where the coke is oxidized to obtain regenerated catalyst. The hydrocarbon trench liquid distributor 2 is shown in more detail in FIG.

2 is an enlarged side view of the lower portion of the apparatus of FIG. 1; FIG. Riser 1 includes inner wall IA, outer wall IB, center IC, and flange I.
D and a narrowed constriction IE. Distributor 2
has a conical element 2A as shown, the tapered end of which is connected to the hydrocarbon liquid introduction means 3, and the thick end of which is disposed a nozzle 2C with a discharge means 2D. There is. The hydrocarbon introduction means 3 are normally connected to the riser 1 by a flange ID. Figure 2 shows nozzle 2C.
A preferred arrangement of the liquid distributor 2 is shown such that the evacuation means 20 are below the regenerated catalyst introduction means 4. The possibility of clogging of any of the nozzles 2C by coke, which may occur in low throughput operations, especially when the hydrocarbon feed rate through the nozzles 2C is low, is reduced if the distributor 2 is arranged in this way. It is thought that the number of cases where the discharge means 20 is located above the regenerated catalyst introduction means 4 is smaller than when the discharge means 20 is arranged above the regenerated catalyst introduction means 4. FIG. 2 shows a side view of three nozzles 20, one central nozzle and two outer circumferential nozzles. The center nozzle is arranged to deliver the hydrocarbon feed liquid so that it rises straight from the nozzle to the central IC of the riser 1. The outer circumferential nozzle has a discharge means 20 in which the combined hydrocarbon liquid coming out from this nozzle is
Preferably, the regenerated catalyst charging means 4 is arranged to impinge on the inner wall IA of the tube 1 downstream of the point where it joins the tube 1. More preferably, the hydrocarbon supply liquid impinges on the inner wall IA at a distance of at least 30.5 meters downstream from the two ears where the regenerated catalyst inlet means joins the pipe 1. Nozzle 2
The hydrocarbon feed rate discharged from C is about 0.3-15.
2 skins/sec, preferably about 1.5 to 6.1 skins/sec
Will. The confluence of hydrocarbons that collide with the inner IA from the outer nozzle at such a speed crushes the wall effect,
Since the wall temperature is lowered, the temperature at any point in the horizontal cross section of the conduit 1 approaches approximately the same temperature. A beneficial effect of the reduction in surface flooding is that overcracking of the hydrocarbon feedstock and the resulting production of dry gas is inhibited. One preferred embodiment of a hydrocarbon feed liquid distributor is shown in more detail in FIGS. 3 and 4.

FIG. 4 shows a truncated cone 2A having a thin lower end and a thicker upper end to which a plate 2B is glued. Here, the plate 2B does not necessarily have to be flat or horizontal, and may be a dome-shaped plate. The diameter of the narrow end is approximately the same as the diameter of the hydrocarbon supply introduction means to which the narrow tip is attached. The diameter of the thicker end is such that it passes through the flange connecting the riser and the hydrocarbon supply cage liquid introduction means and also through the constriction of the riser conduit. The plate 2B has a first circular hole extending through the center of the plate, and a plurality of second holes penetrating the plate arranged at equal intervals along the circumference at a constant radius from the center of the plate. A circular hole is provided. The cylindrical nozzle 2C has an introduction part 2E inserted into the first and second holes, and the hydrocarbon feed liquid exits the nozzle 2C and the distributor 2 through the discharge part 2D. The first nozzle 2C is located at the center of the plate and is arranged at right angles to the plate 2B. That is, the arrangement is such that the vertical center line passes through the centers of the introduction part 2E and the discharge part 2D of the central nozzle 2C.
The hydrocarbon false feed is therefore blown upwardly from this central nozzle into the center of the riser conduit. As shown in FIG. 4, the plurality of second nozzles 2C are arranged in an annular shape around the center nozzle, and the center line passing through the most axis of the second nozzles is the center line passing through the center of the introduction part 2E of the second nozzles. The nozzle is arranged at an oblique angle from the center nozzle at an angle "a" from the central nozzle. The hydrocarbon feed through these nozzles therefore impinges on the inner wall of the standpipe downstream from the nozzle discharge 2D, particularly at least 12 inches downstream from the point where the regenerated catalyst charge joins the riser conduit. Angle “a” is about 100~
It is preferably within the range of 300. Although seven secondary nozzles are shown in the drawings, from three to about three secondary nozzles can be arranged in this manner on plate 2B. The total number of nozzles and internal diameter dimensions are approximately 0.3
~15.2/sec, preferably about 1.5-61 skin/sec
It is assumed that it can be fed at a speed of sec. Another preferred embodiment of the hydrocarbon feed distributor 2 is illustrated in detail in FIGS. 5 and 6. Similar to FIG. 4, FIG. 6 also shows a truncated cone 2A having a narrow end and a thick end with which the plate 2B is fitted. However, in this embodiment, the plate 28 has first holes that pass through the plate 28 and are arranged at equal intervals along a first circumference having a constant radius from the center of the plate 28.
and second circular holes passing through the plate 2B that are arranged at regular intervals along a second circumference (larger than the first circumference) having a larger constant radius from the center of the plate 2B. There is. The introductory part 2E of the yen total/zuru 2C is the first and second
It is inserted into the circular hole, and the hydrocarbon supply blue stream exits from the nozzle 2C and the distributor 2 through the discharge part 2D. 1st
Nozzle 2C is located on the first circumference of the plate and is arranged at right angles to plate 2B. That is, the common vertical center line passes through the centers of the introduction section 28 and the discharge section 2D of each first nozzle. Accordingly, the hydrocarbon feed through the first nozzle is forced upwardly into the center of the standpipe. The second nozzles 2C are arranged on a larger second circumference, and the center line passing through the most axis is mirrored from the first nozzle at an angle "a" from the vertical center line passing through the center of the introduction part 2E of the second nozzle. It is arranged diagonally. Therefore, the hydrocarbon supply liquid passing through these nozzles will collide with the inner wall of the standpipe downstream of the nozzle discharge section 2D, particularly at least 12 inches downstream of point #9 where the regenerated catalyst embedding means joins the standpipe. . Angle "a" is approximately 10-3
It is preferably within the range of 0o. Five first nozzles and one second nozzle are shown, but there are no first nozzles,
The second nozzle can be arranged in about 3 to about 2 increments.

The total number and inner diameter dimensions of the nozzles are such that the hydrocarbon feed liquid can be delivered at a speed of about 0.3 to 15.2/sec, preferably about 1.5 to 6
．． Assume that it is fed at a speed of 1 m/sec. Common features of such embodiments of the invention are: {1} one or more first nozzles are provided at right angles to the disk 2B; (2) riser conduits are also provided away from the first nozzles; [3] Second nozzles arranged on the disk 2B at equal intervals on the circumference thereof are provided so as to face the inner wall of the disk 2B. It is.

The first nozzle is placed at right angles to the disk 2B to avoid dead spaces or slow flow areas in the center of the conduit. As previously explained, the second nozzle necks toward the inner wall of the riser conduit, so that the hydrocarbon feed exiting this second nozzle impinges on the inner wall of the riser conduit. It destroys the inert boundary layer of the high temperature catalyst and reduces the temperature of the conduit wall.
The second nozzles are arranged at equal intervals on the circumference of the disk 2B,
The hydrocarbon feed from the second nozzle therefore impinges evenly around the inner wall of the riser conduit and does not create localized hot spots. The materials constituting the liquid distributor according to the present invention are:
It is capable of withstanding the abrasive effects and sustained conditions of elevated temperatures found in the lower portion of the riser conduit.

In particular, metals such as carbon steel or stainless steel are conceivable. Typically, nozzle 2C is made from 80- to 16-piece pipe, and disk 28 and frustoconical shape 2A are made from 1.3-shaped steel plate. The upper surface of disc 28 preferably has a diameter of 1.3 to 2. It may be covered with refractory concrete to further improve wear resistance. The present invention comprises: 'a) delivering a first portion of a hydrocarbon feed to one or more first nozzles having a first inlet and a first outlet; 'b' second introduction, vertically disposed in the castle, thereby vertically guiding a first portion of the hydrocarbon feed from the first outlet to the center of the catalytic conversion zone; having an opening and a second outlet;
A plurality of catalytic conversion reaction zone arranged in the catalytic conversion reaction zone such that the center line passing through the most axis of the second nozzle is inclined toward the inner wall of the catalytic conversion reaction zone at an angle from the vertical center line passing through the center of the second inlet. delivering a second portion of the hydrocarbon feed to a second nozzle, such that the second portion of the hydrocarbon feed exits the second outlet and impinges on an interior wall downstream of the second outlet; carbonization in a catalytic conversion zone having a center and an inner wall, comprising: and [c} contacting the hydrocarbon complex from the first and second nozzles with a catalyst under conversion conditions; Also included are hydrocarbon feed distribution methods in which the hydrogen feed is injected into contact with the fluidized catalyst.

In one embodiment, the first portion of the hydrocarbon donor is delivered from a single first nozzle; in another embodiment, the first portion is delivered from a plurality of first nozzles. The first and second portions of the hydrocarbon feed are 0.3 to 15.2 m/sec,
More preferably, it is delivered from the first and second nozzles at a rate of about 1.5 to 61 skins/sec. Preferably, the second portion of the hydrocarbon feed exits the second outlet 30. downstream of the second inlet. It collided with the inner wall of the conversion belt castle at two points at a distance greater than the distance of the enemy. The hydrocarbon feed may be in liquid phase, gas phase or liquid phase;
It may be a mixed phase of gas phase, but preferably 177°C~
It is in a liquid phase at a temperature of 371°C. The hydrocarbon mixture is approximately 62
Contact with the high temperature catalyst entering the conversion zone at a temperature of 1-7320°C. Other conversion conditions in the conversion zone include a total pressure ranging from approximately atmospheric pressure to approximately 7.5 mm. and hydrocarbon retention time from about 0.9 sand to 5 minutes, more preferably about 0.
．． 9 sand for 2 minutes. Conversion conditions also include the presence of steam or other vaporous substances that promote fluidization of the catalyst and reduce the hydrocarbon partial pressure to promote cracking reactions.

[Brief explanation of the drawing]

FIG. 1 is a side view of a fluid catalytic cracking apparatus incorporating as one element a hydrocarbon liquid distributor according to the invention; FIG. 2 is a side view of the lower end of the cracking apparatus shown in FIG. An enlarged side view of the lower end showing in detail the alignment of the feed liquid distributor of the riser conduit with respect to other elements of the cracking device: FIG. FIG. 5 is a plan view of another embodiment of a hydrocarbon liquid distributor according to the present invention; FIG. 4 is a cross-sectional view of the hydrocarbon liquid distributor shown in FIG. : and FIG. 6 is a cross-sectional view of the hydrocarbon liquid distributor shown in FIG. 1: riser reactor conduit, 2: hydrocarbon liquid distributor, 3:
Hydrocarbon inlet, 4: Regenerated catalyst inlet, IA: Inner wall, I
B: Outer wall, IC: center, 2A: conical combination, 28: circular plate, 2C: nozzle, 2D: discharge port. 'Nota. / ``Nota.2 f'Yu.3 〆Nota.Yugunota.G'noda.6

Claims (1)

Claims: 1. (a) directing a first portion of a hydrocarbon feed to one or more first nozzles having a first inlet and a first outlet, the first nozzles being connected to a catalytic conversion zone; (b) a second inlet and a second inlet; a second outlet, the center line passing through the long axis of the second nozzle being inclined toward the inner wall of the catalytic conversion reaction zone at an angle from a vertical center line passing through the center of the second inlet; delivering a second portion of the hydrocarbon feed to a plurality of second nozzles disposed within a catalytic conversion zone, the second portion of the hydrocarbon feed exiting the second outlet; and (c) contacting the hydrocarbon feed from said first and second nozzles with a catalyst under conversion conditions. A hydrocarbon feed distribution method in which the hydrocarbon feed is injected into contact with a fluidized catalyst in a catalytic conversion zone having a catalytic conversion zone. 2. The method of claim 1, wherein said first portion of hydrocarbon feed is delivered from a single nozzle. 3. The method of claim 1, wherein the first portion of hydrocarbon feed is delivered from a plurality of first nozzles. 4 said first portion and second portion of hydrocarbon feed are approximately 5-20 ft/sec (1.5-6 m/sec
4. A method according to any one of claims 1 to 3, wherein the hydrocarbon feed rate is from the first and second nozzles, respectively. 5 said second portion of said hydrocarbon feed exits said second outlet;
5. The method of any one of claims 1 to 4, wherein the method impinges on the inner wall at a point about 30.5 cm or more downstream of the second outlet. 6 (a) a frustoconical body having a small diameter end and a large diameter end connected to a hydrocarbon feed inlet; (b) having one or more first through holes and a plurality of second through holes; (c) a circular plate attached to the large diameter end; (c) attached to the first through hole and having a first inlet and an outlet arranged to guide the hydrocarbon feed into the center;
or more first nozzles; and (d) a second outlet attached to the second through hole and arranged to guide the second inlet and the hydrocarbon feed downstream to impinge on the inner wall. a plurality of second nozzles;
a lower end, a cylindrical inner wall, a cylindrical outer wall, a central portion, a hydrocarbon feed inlet provided at the lower end, and a regenerated catalyst inlet, the regenerated catalyst inlet being downstream from the hydrocarbon feed inlet. a hydrocarbon feed distributor for injecting and contacting the hydrocarbon feed to the fluidized catalyst under conversion conditions at the lower end of the riser reactor conduit passing through each of said walls adjacent to said hydrocarbon feed distributor; A first nozzle is disposed perpendicularly to the disc, and a second nozzle is arranged such that a centerline passing through the long axis of the second nozzle is inclined at an angle to a vertical centerline passing through the center of the second inlet. is arranged such that the hydrocarbon feed passing through the second nozzle exits the second outlet, exits the second outlet, and connects the riser conduit downstream from the second outlet. Hydrocarbon feed distributor impinging on the inner wall. 7. A single first through hole was provided in the center of the disk, a first nozzle was attached to the through hole, and a second through hole was drawn in a circle with an appropriate radius from the center of the disk. 7. The hydrocarbon feed liquid distributor according to claim 6, wherein said second nozzle is provided on the circumference of said through hole. 8. The hydrocarbon feed distributor of claim 6 or 7, wherein said angle is between about 10 degrees and about 30 degrees. 9. The hydrocarbon feed distributor of any one of claims 6-8 having from about 3 to about 30 second nozzles. 10. Claims 6-9, wherein the hydrocarbon feed from the second outlet impinges on the inner wall at a distance of about 30.5 cm or more downstream of the regenerated catalyst outlet. The hydrocarbon feed liquid distributor according to any one of the above. 11 A first through-hole is attached to the first nozzle, the first nozzle being equally spaced around a first circle drawn at a first radius from the center of the disk, and a second through-hole. A hole is arranged on the circumference of a second circle larger than the first circle drawn at a second radius from the center of the disk, and a second nozzle is attached to the second through hole. A hydrocarbon feed distributor according to claim 6. 12 the first nozzle is disposed perpendicularly to the disc, and the second nozzle has a centerline passing through the long axis of the second nozzle at an angle with respect to a vertical centerline passing through the center of the second inlet; the hydrocarbon feed passing through the second nozzle exits the second outlet and impinges on an inner wall of the riser conduit downstream from the second outlet;
A hydrocarbon feed distributor according to claim 6 or claim 11. 13. The hydrocarbon feed distributor of any one of claims 6, 11, or 12, wherein said angle is about 10 to about 30 degrees. 14. The hydrocarbon feed distributor of any one of claims 6, 11, or 13 having from about 3 to about 10 first nozzles. 15. The hydrocarbon feed distributor of any one of claims 6, 11, or 14 having from about 3 to about 20 second nozzles. 16. Claims 6 and 11, wherein the hydrocarbon feed from the second outlet impinges on the inner wall at a distance of about 30.5 cm or more downstream of the regenerated catalyst inlet. or the hydrocarbon feed liquid distributor according to any one of paragraphs 15 to 16.