TW476786B - Process and apparatus for feed contacting with immediate catalyst separation - Google Patents

Abstract

A particular arrangement of an FCC unit creates an immediate and sustained gravity separation of catalyst and hydrocarbon vapors in short contact time cracking operation. A transverse feed contactor ejects the mixture of catalyst and hydrocabon vapors transversely into a central portion of a separation vessel for vertical disengagement of catalyst from vapors. The vapors travel upwardly in the vessel into an inertial separator that quickly segregates entrained catalyst from the hydrocarbon vapors and collects separated catalyst at a higher elevation for stripping of adsorbed hydrocarbons from the catalyst.

Description

1 V. Description of the invention (There are many continuous circulation methods using fluidized solids technology, in which at least part of the liquid phase containing the hydrocarbon compound is in contact with the fluidized solid m in the contact zone and the carbonaceous or other fouling substances Deposited on solids. The solids are transported to another zone during the cycle, where the fouling is removed in the regeneration section, or, more specifically, in most cases, by burning in an oxygen-containing medium, the The carbon deposits are at least partially removed. The solids in the regeneration section are then removed and reintroduced in whole or in part into the contact zone. One of the more important methods with this characteristic is the conversion of relatively high boiling hydrocarbons to Fluid catalytic cracking (FCC) process for light hydrocarbons. The hydrocarbon feed is contacted in one or more reaction zones with a granular cracking catalyst maintained in a fluidized state under conditions suitable for the conversion of hydrocarbons. The feed is processed in an FCC-type process, and the feedstock's tendency to produce and produce undesired products results in a novel method that requires the feed to be contacted with a catalyst. The FCC has recently been catalyzed The method of contacting a very short contact time is particularly valued. In US-A 4,985,136, the contact time between the FCC feed and the catalyst curtain (faiiing_curtain) is less than 丨 seconds, and then it is quickly separated. This ultra-short contact time system Improve the selectivity of gasoline generation, while reducing the production of coal coke and dry gas by using a South active catalyst that has been in contact with the feed for a relatively short period of time. The present invention is particularly related to sludge catalysts with thorium activity. Material contact configurations are known from US-A-2,935,466, US-A-4,435,272, US-A 4,944,845, US-A-5,296,131, and US-A 5,462,652. The types of injection required for short contact time configurations are listed above For the reference in the patent, please don't pay attention. The feed can be through a row of the same feed injection stream or borrow -4-This paper size applies the Chinese National Standard (CNS) A4 specification (210 X 297 mm) 2 5. DISCLOSURE OF THE INVENTION (A jet stream is formed by an extended orifice that is in uniform contact with a catalyst stream flowing in a compatible form. The feed injection is set to shoot the feed in a direction perpendicular to the heart motion of the jet stream I. In the relatively thin catalyst belt. In addition to the uniform feed and catalyst contact, short contact time also requires good separation between the halogenating agent and the hydrocarbon. The previous prior art typically introduced the catalyst and vapor mixture to In the conduit that communicates with the downstream separation unit. Therefore, the contact of the hydrocarbon with the catalyst will continue for a substantial period of time when it flows to the separation unit and when it is in the I separation unit. SUMMARY OF THE INVENTION The present invention is to feed a relatively heavy hydrocarbon The configuration of contacting the fluidized catalyst particles for an ultra-short time further limits the contact time between the catalyst and the hydrocarbon. The present invention injects the catalyst stream and the contact vapor together into a substantially horizontal direction to the release under the condition of dilute catalyst phase In this zone, and by immediately removing the cracked vapor from above the dilute phase zone, a rapid separation of the feed from the catalyst stream is provided. The horizontal dilution phase is injected above the combined vapors in the release vessel and the immediate gravity separation of the catalyst from the hydrocarbon vapors is initiated. In this way, a significant portion of the contact between the catalyst and the hydrocarbon is stopped immediately when the catalyst stream is injected into the detachment vessel ^ The contact of the feed and the catalyst stream can occur about the same as the catalyst stream injected into the detachment vessel Location or close to the same location. In this way, the minimum contact time can be controlled from a minimum time from close to zero to a longer time. Unlike previous techniques, the present invention requires maintaining contact when the catalyst and hydrocarbon mixture are moved vertically or horizontally to the separation section together. -5- This paper size applies to China National Standard (CNS) A4 (210 X 297 mm) ^ / 6786 ^ / 6786 A7

Therefore, in a specific example, the present invention is a method for catalytic cracking of a hydrocarbon feed. In this method, the catalyst particles and hydrocarbons are injected from the injection center = the catalytic thousands of universal injections to the catalyst particles in the separation zone where m is injected = Sheung Shui. In the disengagement zone, the landing point and the collection zone Wanji landed 5 inches; the distance between the feet provides continuous catalyst and hydrocarbon vapor separation :: This method collects the rising vapor and ribbon particles from the upper part of the emission zone, and Conveyed to the inertial separation zone. The inertial component ′ 郃 particles = entrained catalyst, and provides separated vapor flow and separated catalyst:]. This method recovers hydrocarbons from the lower part of the separation zone and the separated vapor stream. On the eighth type, the jet of the hydrocarbon-containing feed is injected in a mainly transverse direction into the flowing layer of catalyst particles upstream of the> shot point and around the plutonium zone or outside the escape zone. A particularly useful form of the present invention uses a tube as the location of the nozzle arrangement of the distributor for contacting the hydrocarbon-containing stream with the falling layer of the particulate matter. The jet of hydrocarbon-containing feed is injected into the catalyst particles. The layer generally occurs in a sealed conduit, but close to the conduit and enters the exit of the trough. For the practice of the invention, the position of the dispenser in the riser will typically allow the fluid and solid mixture to be drained directly from the dispenser into the release container at the appropriate height. The riser distributor is configured to fit tightly near most riser and breakaway container connections. In a specific example of the apparatus, the present invention includes a release vessel portion and a catalyst and a feed contactor for injecting feed and catalyst from an injection point into the release vessel portion in a substantially horizontal direction. The feed contactor injects a hydrocarbon-containing feed into the catalyst's flowing stream, and supplies the feed and catalyst to the injection point. One person is below the part of the container, and at least 5 -6- below the injection point. This paper size applies the Chinese National Standard (CNS) A4 specification (210X297 mm) 476786 A7 'B7 V. Description of the invention (4) feet collection The container part collects the catalyst compact bed from the container part. An inertial separator above the detachment vessel portion is in direct communication with the upper portion of the detachment vessel portion, and the hydrocarbons are separated from the catalyst particles raised together with the hydrocarbon from the detachment vessel portion. A catalyst outlet defined by the inertial separator recovers the separated hydrocarbons from the inertial separator. Brief Description of the Drawings Figure 1 is a schematic illustration of a FCC device incorporating the short contact time configuration of the present invention. FIG. 2 is a schematic cross section crossing the line 2-2 of FIG. 1. FIG. Figure 3 is a schematic illustration of an FCC device incorporating another short contact time configuration of the present invention. FIG. 4 is a schematic cross-section across line 4-4 of FIG. 3. Fig. 5 is a cross-sectional view of a portion of a riser catheter including a contactor used in the present invention. FIG. 6 is a cross-section of the riser conduit portion taken along line 6-6 of FIG. 5. FIG. FIG. 7 is a front view of the feed distributor on line 7-7 of FIG. 5. FIG. The main components are represented by the symbol 10 reactor 14 collection container portion 11 detached container portion 14, collection container portion 11 'detached from container portion 15 riser 12 separator container portion 15' riser section 13 separator 16 riser nozzle 13, separation zone 16 '' Catalyst conduit This paper size applies the Chinese National Standard (CNS) A4 specification (210 X 297 mm) 476786 A7 B7 V. Description of the invention (5 17 feed injection nozzle 31, nozzle 18 injection point 32 nozzle 18, injection point 33 bed 19 open volume 33, bed 20 open volume 34 riser 21 catalyst interface 35 bottom 21, higher catalyst interface 36 conduit 22 compact bed 38 JLT 22, extended bed section 38 丨 outer riser 22 ', compact bed 39 opening 23 nozzle 40 Separation fence 24 Distributor 41 Limiting opening 25 Grid 42 Second section 26 Nozzle 43 Baffle 27 Nozzle 44 Central section 28 Frustum 46 Catalyst tube 29 Arm 111 Flange 29, Arm 113 Chute 30 Opening 114 Exit · 30 丨Opening 115 Contactor 31 Out π 123 Nozzle Detailed description of the invention The invention can be combined with any type of granular material Use. This material is suitable for China National Standard (CNS) A4 size (210X 297 mm) 476 786 In this paper scale special -8-

DESCRIPTION OF THE INVENTION (Boundary fluid materials can be inert or reactive in the presence of a variety of materials. There are a wide variety of inert and catalytic materials suitable for use in the present invention. For example, in the destruction of steam contacts, suitable inert materials include alpha oxidation oxide. The applications of this method may include any well-known catalysts used in fluid catalytic cracking techniques. These compositions include amorphous clay-type catalysts, most of which have been oxidized and broken down with high activity crystalline oxides or contain Wei Wei Replaced by catalysts. Beachstone-containing catalysts are more amorphous type catalysts due to their higher intrinsic activity and their higher resistance to high temperature exposure to steam and deactivation of metals contained in most of the original families. Better. The most commonly used crystalline oxidized salt of travertine, and it is usually dispersed in a porous inorganic support material such as silica oxide, or zirconium. These catalyst compositions may be sold. The above frozen Stone contains I. It is preferred that the sludge catalyst in the method of the present invention has a zeolite content of 25-80% by weight of the catalyst. The soil is stabilized, and the JL contains fetal soil from 0% by weight. Although the present invention is mainly designed for use in the Fcc unit, it can also be used to attempt to contact a hydrocarbon-containing stream with a fluidized particle stream for a short time. Any procedure. Types of procedures to which the present invention may be useful include contacting the catalyst with residual feed and contacting feeds with high calendars with high temperature inert or destructive catalytic particles. A suitable liquid medium of the present invention includes Become a liquid and enter the dispenser 'and further evaporate by contact with granular material <any liquid stream. The contact disrupting feed will include high levels of metal and coal coke with stagnation points that extend over a wide range Refractory original: For example, '-A typical original family has a boiling point from η6, 815β (: 收. The boiling point of printing, and more than-half of the liquid volume has a boiling point higher than 100 (TF. Off

476786 A7

Raw materials suitable for processing in the FCC process' using the method of the present invention include conventional FCC feeds and relatively small or residual feeds. The most commonly known feed is vacuum gas oil ', with a typical loading point from 343. _5 hungry_. Assist T) 'and a hydrocarbon material prepared by vacuum consideration of atmospheric residues. The coal coke precursors in these sections and the heavy metals that deactivate the catalyst are generally not high. Heavy or residual feeds, that is, those with a higher boiling point than ⑽⑽ 卞), and feeds with a high metal content, also have increased uses in Fcc units. When used in catalyst operation, both metal and coal char will deactivate the catalyst by blocking the active sites on the catalyst. To overcome this deactivation, the coke can be removed to a desired level via regeneration. Figure 1 shows the Fcc configuration set up according to the invention. The Fcc arrangement shown in FIG. 1 is composed of a reactor 10 including a tritium container portion u, a tritium container portion 14 and a separator 13. The separator 13 includes a separator container portion 12 and a riser 15. This allowed the catalyst to be circulated and the feed contacted in a manner described later. Turning next to the operation of the reaction zone, fresh regenerated catalyst, used catalyst, or a mixture thereof enters the reactor through a nozzle 16 which is typically in communication with the end of the regenerated catalyst standpipe. The feed is injected into the riser nozzle 16 via a feed injection nozzle 17 which is in contact with the catalyst (preferably in contact with the catalyst via a contactor as described further herein). After or after the contact between the feed and the smoke, the feed and the catalyst particles enter the escape container portion 11 from the injection puppet. The contact of the catalyst with the feed will result in a concentrated stream of catalyst flowing into the escape vessel portion 11 along a substantially horizontal flow path. Will essentially water -10-

476786 A7 — 'B7 V. Description of the invention (8) Flat flow control is defined as the flow path with at least the main horizontal component. The main direction of the catalyst stream as it enters the exit vessel will primarily determine the orbit of the feed and the hydrocarbon stream. Therefore, the hydrocarbon stream will be introduced into the release vessel at an angle below 60 ° shown as A in FIG. 1, while ensuring the momentum of the catalyst allows the mixture of catalyst and smoke to move through the release vessel portion in a substantially horizontal direction. 11. Substantially horizontal emissions from the disengagement point facilitate the rapid disengagement of vaporous hydrocarbon streams from relatively heavy catalyst particles. The rapid detachment also requires a vertical space for the ascending vapor to pass upward through the detachment container 11 without restriction. For this reason, the part detached from the container will have a substantially open volume 19 above the injection point, and perhaps more importantly an open volume 20 below the injection point. The open volume 20 is defined as the area of the thin catalyst density above the catalyst interface 21, and it is shown as the dimension B in FIG. Dimension B will be at least 1.5 meters, and more typical from 2 to 3.6 meters. Dilute phase conditions refer to catalyst densities below 300 kg / m3, and densities below 150 kg / m3 will be more typical. The catalyst density in open volumes 19 and 20 will vary depending on how close the feed and catalyst contact points are. Generally the density of the open volume will not exceed an average value of 80 kg / m3; and typically it will have an average catalyst density of less than 48.4 kg / m3. The catalysts from the open volumes 19 and 20 are collected in a dense bed 22 in a collection container section 14. Dense phase conditions are characterized by the apparent bulk density of the catalyst in the range from 240 to 800 kg / m3. Therefore, the compact bed 22 in the collection zone typically holds the catalyst particles at a density of at least 240 kg / m3 and the catalyst particles at a density of more than 730,000 kg / m3. On the part of the container -11-This paper size is in accordance with China National Standard (CNS) A4 (210 X 297 mm) '--- A7

The distance B can also be used as a sinking area for the catalyst to escape from the rising vapor and settle. The collection container portion 14 may be provided as a stripping zone for recovering the entrained and adsorbed hydrocarbons from the 14 K chelating agent entering the collection container portion 14. The stripping gas enters the collection container portion 14 through the nozzle 23 and the distributor 24. The dispersed stripping gas, such as steam, rises through the catalyst. A series of grids 25 can provide for the redistribution of the vapor k and the stripped hydrocarbons as they pass upward through the bed 22. The nozzle 26 removes the stripped catalyst for regeneration in a regeneration vessel (not shown) and / or recycles to the nozzle 6 to bring the catalyst into contact with the feed. The optional addition of thermal regeneration catalyst to bed 22 can promote stripping by increasing the temperature in the stripping zone. The hot catalyst can enter the stripping zone above the bed interface 21 through the nozzle 27. Alternatively, the extended bed portion 22 having a higher catalyst interface 2Γ may be maintained so that the dense-phase catalyst is maintained above the entry point of the regenerated catalyst through the nozzle 27, and the restriction is between the injection point i 8 and the bed 21 ' Provides minimum breakout length. It is also possible to isolate the recovered stripped hydrocarbons from the lower part of the bed 22 through a baffle (not shown). Separation of the stripped hydrocarbons can provide different product streams for downstream separation and recovery. The longer contact time of hydrocarbons entering the collection zone can substantially alter the properties of cracked smoke recovered from this zone. The individual recovery of the stream from the stripping zone can facilitate the independent recovery of the separated product stream from the upper part of the separation vessel. However, the stripping medium and the stripped hydrocarbons will generally rise through the detachment vessel portion 11 &apos; and combine with the detached hydrocarbons entering simultaneously from the nozzle 16 and the catalyst stream. When the vapor and entrained catalyst rose through the open volume 19, it was truncated. -12- This paper size applies to China National Standard (CNS) A4 (210X297 mm)

The transition section of the shape of the cone 28 reduces the dynamic area of the fluid flow a, and increases the velocity of the gas as it ^ ③ 15 8 乂. The conditions in the open volume 19, cone 28, and riser 15 are generally referred to as rapid fluidization conditions, in which the catalyst's upward conveying speed can range from 6 to 18 meters per second, and the density ranges from 65 to 550 kg / m3. Rising hydrocarbons and any additional entrained catalyst will rise up into the inertial separation device provided by a pair of arms 29 each having a tangential guide opening 30. The arm 29 provides inertial separation by the centripetal acceleration of the relatively heavy catalyst particles, while quickly removing most of the catalyst from the money. The use of a tangential opening π to provide centripetal or cyclonic separation is described herein, and & does not mean to exclude other inertial separation devices, such as those that use particles to separate from the emission of hydrocarbon vapors. The cracked hydrocarbons with a small amount of catalyst leave the separator 13 via an outlet plutonium. In most cases, the hydrocarbon vapor from the outlet 3 will undergo further separation to recover traces of catalyst particles. Cyclone separators are usually used to provide secondary recovery of residual catalyst particles. The catalyst particles recovered from the other separators can be returned to the collection container portion 14 via the nozzle 32. After any additional catalyst recovery, the product is typically sent to a separation zone (not shown) 'to remove light gases and heavy hydrocarbons from the product. The catalyst recovered from the inertial separator 13 is collected in a bed 33 to be returned to the bed 22 in the collection container portion 14. The catalyst may pass from the bed 33 through the one or more inner or outer risers 34 to the collection container portion 14. Figure 1 shows the configuration of the internal riser 34 which isolates the catalyst from the open volumes 19 and 20 of the detached container section and returns it from the bed 33. The bottom 35 of the riser 34 is typically buried -13- This paper size is applicable to the Chinese National Standard (CNS) A4 specification (21 × 297 mm) 476786 Α7 Β7 V. Description of the invention (μ into the bed 22. Put the riser The bottom 35 is buried to prevent the stripped vapor from flowing back through the riser into the separated vapor collected at the top of the separation zone 131. The inner riser 34 has a clear path left for the injection of hydrocarbons and catalyst particles as they are The configuration used when the injection point 18 enters the detached container portion 11. As shown more clearly in FIG. 2, the interval of the internal risers 34 is increased in the area of the nozzle 16 to provide an interval equal to the size C between the risers 34. Size c is preferably at least equal to the diameter of the nozzle 16. With this configuration, the injected hydrocarbon and catalyst particles have an unobstructed orbital path extending from the size T to at least the center of the part detached from the container. The form of the inertial separator 13 And the return of the catalyst to the collection container portion 14 can be formed in a variety of different ways. Figure 3 shows the use of a downwardly extending conduit% and a separation enclosure 40 to improve the recovery of the separated catalyst from the inertial separation device, and The catalyst is returned to the compact bed 22 by an external standpipe 38. Another configuration. The apparatus of FIG. 3 operates in a similar manner to the apparatus described with respect to FIG. 1. The main difference is that when the steam is leaving the vessel section u, An additional change in the direction of the vapor is introduced when passing in the middle direction, and the catalyst particles are further separated from the hydrocarbon vapor before the mixture leaves the separation zone 13 *. More specifically, when the vapor flows to the opening that receives the separated hydrocarbon vapor 3-9 The hydrocarbons are separated from the entering catalyst particles from the injection point 18 'into the separation vessel portion η. The opening 39 is provided as a separator inlet, and it faces the side opposite the catalyst particles and the hydrocarbons injected through the injection point 18, The detachment zone on the side. In this way, the hydrocarbon leaves the detachment zone on the side opposite to the catalyst particles and the hydrocarbon injection side. -14-This paper size applies the Chinese National Standard (CNS) A4 specification (£ 797 mm) · ^ —— __ 476786 A7 B7 V. Description of the invention (The hydrocarbons and entrained catalyst from opening 39 continue to pass upward through the riser section 15f. The arm 29 'also passes through the opening 30, The catalyst and entrained catalyst particles are discharged tangentially. The enclosure 40 provides a restricted opening 41 for the recovered steam to enter the separation zone 13, the second section 42. The recovered hydrocarbons and any residual catalyst also pass through the nozzle 3 Γ leaves the separation zone 13, and the outer tube 38 is collected from the catalyst bed 3 3 by the inertial separation zone 13 to recover the catalyst. The riser 38 allows the catalyst to bypass the detachment container section 丨 and enter the collection container section 14 The dense bed 22 ,, middle. The external riser 38 makes the detached container part 11 yuan fully open for the hydrocarbon vapor to escape from the catalyst stream. The open section of the separation zone can be further isolated to limit the flow of hydrocarbons from the catalyst particles. Separation. As shown in Fig. 4, a pair of baffles 43 may be provided near the catalyst duct 16 'in the center portion 44 which discharges the catalyst particles and the feed mixture to the detachment vessel portion?. The detached container portion u may be further modified to provide a conduit for returning catalyst particles located outside the central portion 44. The catalyst duct 46 may be provided in a sector area outside the baffle 43. The method and apparatus of the present invention can initially contact the feed with a regenerated catalyst, a carbonization catalyst, or a mixture of both. This method can use any type of regeneration to remove coal coke. Coal coke removal, which is usually operated to completely remove coal coke from the catalyst, is generally referred to as "complete regeneration". Complete regeneration ^ Removed from the catalyst to an amount of less than 0.2% by weight, or preferably less than 0.1% by weight, and / or to less than 0.05% by weight, and better. "&Lt; Coal char regeneration catalysts will have substantially higher temperatures than carbonization catalysts. 通 -15-

The regenerated catalyst entering the reed nozzle 16 will have a temperature in the range from 590 to 760 ° C, and a temperature in the range from 65 to 7600c is more typical. Once the catalyst mixture is in contact with the feed, the catalyst will accumulate coal coke on the catalyst, pellets, and have a lower temperature. The temperature suspension of the carbonization catalyst will be in the range from 480 to 620 ° C, but its temperature will vary depending on its source. The preferred riser and feed injection configuration for this month is shown in Figure 5. Figure 5 illustrates a contactor that atomizes the feed into a stream of fine droplets. The flange 1Π at the end of the feed injection nozzle 11 generally holds the contactor 115 in the feed injection nozzle 17. The stream generated by the contactor 115 as a whole provides a linear array of catalysts in contact with the falling curtain of the catalyst formed by the chute 113 &lt; outlet 114. The contact of the feed with the catalyst causes rapid evaporation and high-speed discharge of the catalyst into the release vessel. The contact between the feed and the catalyst cracks the heavier hydrocarbons into lighter M and generates coke on the most active catalyst section on the catalyst. The lateral contact of the feed with the vertically falling catalyst curtain creates a favorable orbit for the catalyst and feed mixture to enter the release vessel. The feed is in contact with the curtain of falling catalyst in the lateral direction, and it is better to get rapid contact between the feed and the catalyst particles. For the purpose of this note, the wording "horizontal contact" means that the feed does not flow parallel to the direction of the curtain. After the jet of smoke is injected, the catalyst particles typically flow through the mouthpiece 17 below 15 meters and preferably below 0.3 meters before being injected from the injection point into the detachment zone. As shown in Figs. 5 and 6, the chute 113 is fixed inside the nozzle 16, and the outlet 114 generally has a straight line shape. The chute will usually be equal to or greater than the spray -16-

476786 A7 B7 V. Description of the invention (the width of about half of the width of the nozzle 16. The catalyst self-control valve for discharge, typically a slide valve (not shown in the figure), enters the nozzle 16. The control valve regulates the catalyst into the slide The flow rate of the tank 113. The speed of the catalyst discharged from the outlet 114 can be controlled by adding fluid upstream of the chute 丨 13. The contactor 115 will generate a spray form compatible with the shape of the falling curtain. In the case of the linear shape depicted in the figure, the feed syringe will generally produce a nebulized liquid in a horizontal form. Therefore, in a typical configuration, the feed is discharged in a substantially lateral direction relative to the catalyst curtain. The lateral contact indicates that the main direction of the catalyst flow includes an angle between the main direction of the contactor 115 injecting the feed into the catalyst layer or curtain is at least 3G., And at least 45. Preferably, the feed is vertical. Flow: Better contact with the downward moving curtain of the catalyst. When in contact with the falling curtain of the catalyst, the feed will typically have a speed greater than 0.3 m / s: between 150 and 320 Temperature in the range of C. ， The size of the nozzle of the contactor 115 can be made to produce a jet stream with a fluid velocity in the range of 9 to 12 () meters per second outside the opening, and a speed of 30 to 90 meters / It will be better in the range of seconds. According to typical coffee practice, ^ is to leave the mouth of the contactor 115 with a spray. By giving sufficient energy to the liquid, the feed material is dispersed into fine droplets. -In some cases, some gaseous diluent, such as steam, will be discharged into the feed through the orifice, and adding sample to it will promote the atomization of the feed. Typically, the The minimum amount of gaseous substance f is usually equal to about 0.2% by weight of the combined liquid sub-state mixture, mixed with the liquid. Typical: -17-

V. Description of the invention (15 A7 B7 How to add steamed milk is sufficient to combine the gaseous and liquid mixtures below the weight percent. For most liquids, atomization will produce droplets in the size range from 50 to 750 microns. Hui and Ding Kshen passed the linear linear array of nozzles 123 on the front side of the contactor 115. Orienting the nozzles 123 to position the atomized mixture of the fluid closer: The nozzles are directly injected from the contactor 115 in a straight flow The nozzles, which are located closer to the outside of the array, can be tilted at an angle of '23' to orient the atomized liquid of the King of Fire in a wider form, and maintain a uniform interval between the jets. .The nozzle 123 can be tilted at an angle in this way, and it can contain any length or shape of the catalyst flowing form or catalyst point-18-This paper size applies to China National Standard (CNS) A4 (210 X 297 mm)

Claims (1)

A hydrocarbon-catalyzed fluidized catalytic cracking clay A 硪 Wanfa Baohong · a) The jet of the hydrocarbon-containing feed is located in the main lateral direction, upstream of the point, around the escape zone or in the escape zone:剂 隹 b) The catalyst particles and hydrocarbons are injected from the injection point into the disengagement zone with a universal direction of water,,, and, wherein the disengagement zone has above and below the injection point. And the average catalyst density is lower than 80 kg / m3 = the open volume; the collected catalyst particles are collected in the collection area below the injection point, and maintained in the separation area between the injection point and the collection area A settling distance of at least meters, wherein the collection zone has a catalyst density of at least 24 kg / m3; d) collecting rising vapor and entrained catalyst particles from a substantially open volume above the shot point, and lifting the vapor And the entrained catalyst particles are transported to the inertial separation zone, and the catalyst 'f' is separated from the rising vapor to provide a separated vapor stream and the separated catalyst; and e) from the separation zone Portions separated vapor stream and recovery of hydrocarbons. 2. The method according to the scope of the patent application, wherein the hydrocarbon recovered from the lower part of the separation zone enters the inertial separator and is recovered as a part of the separated vapor stream. 3. The method of claim 1 in which the separated catalyst is collected in a common stripping zone together with the dropped catalyst. 4. The method according to item 1 of the scope of patent application, wherein the separated catalyst -19- This paper size is applicable to China National Standard (CNS) A4 specification (210X297 mm) 476786 It is collected above the escape area and enters the collection area downwards in a manner isolated from the rising vapor. 5. The method according to item 2 of the patent application, wherein the injection of a jet of a hydrocarbon-containing feed into the flow layer of the catalyst particles occurs in a sealed conduit, and after the injection of the jet of hydrocarbons, the catalyst particles The injection point flows below 5 meters through the catheter before entering the detachment zone. 6. The method according to item h of the patent application, wherein a regenerated catalyst stream enters the detachment zone or the collection zone below the injection point through the regenerated catalyst inlet, and the sedimentation of the catalyst occurs in the settling zone extending below the regenerated catalyst inlet in. 7. If the method is the oldest in the scope of patent, the rising steam and entrained catalyst particles enter the inertial separator through the opening facing the separator inlet on the side of the separation area opposite to the side where the catalyst particles and smoke are injected. A device for quickly contacting a granular catalyst with a hydrocarbon-containing feed, including: a part of a container that is separated from the container; a device for injecting a hydrocarbon-containing feed into a catalyst flow stream, and The injection point defined by the catalyst free-feeding contactor is injected in a substantially horizontal direction into the catalyst and the second contactor in the part of the detached container, wherein the catalyst and the feed contactor feed the hydrocarbons at a temperature relative to the catalyst flow. The position upstream of the injection point is inserted into the fluidized layer of the catalyst in a substantially transverse direction; and the general position is below the part of the container and at least -20 below the injection point 476786 A8 B8 C8 The collection of 1.5 meters used to collect the catalyst, and the collection in the bed was full of tears. One was in the detached container part, the team was in the state of Shao Wei, Qiu Tingxiang chanted man-hours, and the detached container part The upper part is in communication with each other, and the inertia separator that separates hydrocarbons from blood and π ascending from the part of the container. The inertia separator is used to recover eight σ from the inertial separator. 〇9. The device according to item 8 of the patent application, wherein a plurality of catheters extend vertically through the disengagement section and are spaced apart in the direction so as to leave at least one-half diameter clear track of the disengagement container section before the injection point. Η). For example, the inventor of claim 8 in which the inertial separator defines a horizontally protruding inlet on the side of the separation zone between the open soil and the side of the catalyst particles and hydrocarbons that are invaded. -21-This paper size applies to China National Standard (CNS) Α4 size (210 X 297 mm)