Apparatus and method for dispensing quench fluid

Abstract

A method of distributing a quench fluid into a product stream includes contacting a feed stream with a catalyst stream to convert the feed stream into a product. The quench fluid is ejected from the first distributor through at least one first opening centered on a first radial position and from the second distributor through at least one second opening centered on a second radial position different from the first radial position into the product stream. Preferably, the catalyst is separated from the product stream prior to quenching. The method may include a first set of first dispensers and a second set of second dispensers.

Description

[0001] Priority declaration

[0002] This application claims priority to U.S. Provisional Application No. 63 / 355,131, filed on June 24, 2022, which is incorporated herein in its entirety. Technical Field

[0003] The field relates to the reaction of a feed with a fluid catalyst. In particular, the field relates to the distribution of a quench fluid into a product stream. Background Art

[0004] Light olefin production is critical to producing enough plastics to meet global demand. Alkane dehydrogenation (PDH) is a process in which light alkanes such as ethane and propane can be dehydrogenated to produce ethylene and propylene, respectively. Dehydrogenation is an endothermic reaction that requires external heat to drive the reaction to completion.

[0005] Dehydrogenation catalysts may utilize molecular sieves or amorphous materials to incorporate the dehydrogenation metals. The catalyst must be sufficiently robust and appropriately sized to withstand the attrition expected in the fluidized system.

[0006] In a PDH reaction with a fluidized catalyst, coke can be deposited on the catalyst while catalyzing the reaction. The catalyst can be regenerated in a catalyst regenerator by burning the coke from the catalyst in the presence of oxygen. The hot regenerated catalyst can then be transferred back to the reactor to catalyze the reaction. If insufficient heat is provided to drive the endothermic reaction, olefin production may be affected.

[0007] Both catalytic reaction and thermal cracking reaction may occur in a catalytic reactor at high temperature. The selectivity of the catalytic reaction to the desired product (such as propylene) is higher than that of the thermal cracking reaction. It is necessary to be more careful to maximize the catalytic reaction relative to the thermal cracking reaction to improve the selectivity to propylene. When the catalyst is separated from the product, the product can still be at high temperature. The conditions at this time can be conducive to thermal cracking reaction rather than catalytic reaction. The reactor product can be quickly cooled by quenching to terminate the thermal cracking reaction, and the thermal cracking reaction can crack the propylene product into undesirable lighter gaseous products.

[0008]

[0006] Therefore, there is a need for improved methods of contacting a catalyst with a quench fluid during a fluidized catalytic reaction process. Summary of the invention

[0009] The present disclosure relates to a method for distributing a quenching fluid into a product stream. The method includes contacting a feed stream with a catalyst stream to convert the feed stream into a product. The quenching fluid is sprayed into the product stream from a first distributor through at least one first opening centered on a first radial position and from a second distributor through at least one second opening centered on a second radial position different from the first radial position. Preferably, the catalyst is separated from the product stream before quenching. The method may include a first group of first distributors and a second group of second distributors, the first group of first distributors having at least one first opening centered on a first radial position from a container center, and the second group of second distributors having at least one second opening centered on a second radial position different from the first radial position from a container center.

[0010] Other details and embodiments of the invention will become apparent from the following detailed description of the invention. BRIEF DESCRIPTION OF THE DRAWINGS

[0011] Figure 1 is a schematic diagram of the conversion unit disclosed in the present invention;

[0012] Figure 2 The data is taken at section 3-3. Figure 1 An enlarged partial plan view;

[0013] Figure 3 for Figure 2 An end view of a distributor; and

[0014] Figure 4 The data is taken at section 3-3. Figure 1 An enlarged partial plan view.

[0015] definition

[0016] The term "downstream communication" means that at least a portion of the fluid flowing to the body in the downstream communication can operatively flow from the object in fluid communication therewith.

[0017] The term "upstream communication" means that at least a portion of the fluid flowing out of the body in the upstream communication can be operatively flowed to the object in fluid communication therewith.

[0018] The term "direct communication" means that the fluid flows from the upstream component into the downstream component without passing through any other intervening container.

[0019] The term "indirect communication" means that the fluid flow from the upstream component enters the downstream component after passing through an intervening container.

[0020] The term "bypass" means that the object loses downstream communication with the bypassed body at least within the scope of the bypass.

[0021] As used herein, the term "predominantly" or "majority" means greater than 50%, suitably greater than 75%, and preferably greater than 90%. DETAILED DESCRIPTION

[0022] In a fluidized PDH reactor, the dehydrogenation catalyst and the olefin product gas are separated from each other in a primary catalyst separator. More than 90 wt% of the dehydrogenation catalyst may be separated by the primary catalyst separator. Quench injection can be used to cool down the reactor effluent as quickly as possible at the outlet of the primary catalyst separator to maintain target product selectivity and minimize propane consumption. Ensuring good atomization of the fluid to adequately distribute the quench fluid for good contact with the product gas to adequately reduce its temperature is a challenge due to the large cross-sectional area of ​​the conduit transporting the product gas and the entrained catalyst remaining from the initial separation, and the high velocity of the product gas.

[0023] PDH catalyst is used in the dehydrogenation process to catalyze the dehydrogenation of alkanes such as propane, isobutane and normal butane into olefins such as propylene, isobutylene and normal butene, respectively. The conditions in the dehydrogenation reactor may include a temperature of 500°C to 800°C, a pressure of 40kPa to 310kPa and a catalyst to oil ratio of 5 to 100. The dehydrogenation reaction can be carried out in a fluidized manner so that the gas is distributed to the reactor in a manner that the dehydrogenation catalyst is lifted in the reactor vessel while catalyzing the dehydrogenation of the alkanes, and the gas may be a reactant alkane with or without a fluidizing inert gas. During the catalytic dehydrogenation reaction, coke is deposited on the dehydrogenation catalyst, resulting in a reduction in the activity of the catalyst. The dehydrogenation catalyst must then be regenerated.

[0024] Figure 1 An exemplary PDH reactor 12 is shown in FIG. The PDH reactor 12 may include two chambers: a reaction chamber 14 and a separation chamber 26. A feed line 10 may load a feed stream into the reactor 12. The feed stream may primarily contain propane or butane, but other alkanes such as ethane may be present in the feed stream together with or in place of other alkanes. Any feed distributor may distribute the feed stream to the reactor 12. A dome-shaped reactant distributor 32 or a pipe grid distributor may be utilized in the reaction chamber 14 of the reactor 12. The described dome-shaped reactant distributor 32 receives a gaseous feed stream and distributes the feed stream through a nozzle in the top dome of the dome-shaped reactant distributor 32 to distribute the feed stream over the entire cross-section of the reaction chamber 14. It is contemplated that other fluidizing gases may also be used to promote fluidization in the reaction chamber 14. In one embodiment, the distributed feed stream rises in the reaction chamber 14 and the reactor 12.

[0025] The recycle catalyst conduit 34 has an inlet 35 located in the separation chamber 26 and an outlet including a first catalyst inlet 39 in the reaction chamber 14. The recycle catalyst conduit 34 conveys a first recycle spent catalyst stream that has not yet undergone regeneration from the separation chamber 26 to the reaction chamber 14 through the outlet and the first catalyst inlet 39. The first catalyst inlet 39 provides spent catalyst to the reaction chamber 14.

[0026] To supply additional heat and catalyst to the reaction chamber 14, the second catalyst inlet 43 delivers a second catalyst stream to the reactor 12. The regenerated catalyst conduit 16 has an inlet 17 located in the regenerator 20 and an outlet connected to the second catalyst inlet 43 in the reaction chamber 14. The regenerated catalyst conduit 16 delivers the second regenerated catalyst stream from the regenerator 20 to the second catalyst inlet 43 through the outlet. In one embodiment, the feed stream may be contacted with the second catalyst stream after contacting the feed stream with the first catalyst stream.

[0027] The regenerated catalyst has just undergone combustion regeneration and the average temperature is very hot and active because the coke deposits have been burned from the catalyst surface. Therefore, in the reaction chamber 14, the feed stream is provided with additional enthalpy and catalyst to catalytically convert alkanes to olefins, typically propane to propylene. The average temperature of the second catalyst stream can be 500°C to 900°C. Therefore, the temperature of the reaction chamber 14 can be 400°C to 800°C.

[0028] In the reaction chamber 14, the feed stream contacts the first and second catalyst streams mixed together, and the reactant alkane undergoes conversion to olefins, typically propane to propylene. The feed stream and catalyst stream rise in the reaction chamber 14 of the reactor 12, driven by the feed stream continuously entering the reactor through the reactant distributor 32. At the interface 44, the fluid dynamics change from a catalyst dense phase below the interface to a fast fluidized flow regime above the interface. The catalyst density in the catalyst dense phase is at least 200 kg / m 3 (12.5lb / ft 3 ); and the catalyst density in the fast fluidized flow state is at least 100 kg / m 3 (6.3lb / ft 3 ). The superficial velocity of the feed stream and the first and second catalyst streams in the reaction chamber 14 will typically be at least 0.9 m / s (3 ft / s), suitably at least 1.1 m / s (3.5 ft / s), preferably at least 1.4 m / s (4.5 ft / s) to 2.1 m / s (7 ft / s) to provide a fast fluidized flow regime. In the fast fluidized flow regime the reactant gases and catalyst rise, wherein the catalyst can slide relative to the gas, and the gas can take an indirect upward trajectory.

[0029] The dehydrogenation catalyst can be any one of a variety of catalysts suitable for fluidized dehydrogenation units. The selected dehydrogenation catalyst should minimize cracking reactions and be conducive to dehydrogenation reactions. Suitable catalysts for use herein include amorphous materials or molecular sieves that can be dispersed in porous inorganic carrier materials such as silica, aluminum, zirconium or clay. Exemplary embodiments of the catalyst include crystalline silica-alumina or silica-alumina-phosphate as the main active component, matrix, binder and filler.

[0030] The matrix component may include amorphous alumina or silica, and the binder and filler provide physical strength and integrity. Silica sol or alumina sol may be used as a binder, and kaolin may be used as a filler. The catalyst particles may have a nominal diameter of 20 microns to 150 microns, with an average diameter of 70 microns to 90 microns.

[0031] The dehydrogenation catalyst may support a dehydrogenation metal. The dehydrogenation metal may be one or a combination of transition metals. A noble metal may be a preferred dehydrogenation metal; however, a IIB or IIIB metal may be a suitable dehydrogenation metal, alone or in combination with other dehydrogenation metals. Iron, tungsten, gallium, copper, zinc or zirconium, alone or in combination with each other or with a noble metal, may be a suitable dehydrogenation metal. In addition to the catalyst, a combustion promoter may also be utilized. The metal may be incorporated into the lattice structure of the molecular sieve.

[0032] The acid function of the catalyst should be minimized to prevent cracking and facilitate dehydrogenation. Alkali metals and alkaline earth metals may also be included in the catalyst to reduce the acidity of the catalyst. Rare earth metals may be included in the catalyst to control the activity of the catalyst. Metals may be incorporated into the catalyst at a concentration of 0.05 wt % to 10 wt %. With respect to noble metals such as platinum, it is preferred to use 0.05 wt % to 2 wt % of the noble metal.

[0033] The feed stream lifts the first catalyst stream mixed with the second catalyst stream upward in the reaction chamber 14 while the alkanes are converted to olefins in the presence of a dehydrogenation catalyst which gradually becomes a spent catalyst due to the agglomeration of coke deposits on the catalyst. A fluidizing inert gas may be distributed to the reaction chamber to help lift the mixture of catalyst and reactants upward in the reaction chamber 14. The reactant gas is converted to a product gas while rising in the reaction chamber 14. The mixture of gas and catalyst rises from the reaction chamber 14 through a frustoconical transition section 45 to a transport riser 46 having a diameter smaller than the diameter of the reaction chamber 14. The separation chamber 26 is connected to the downstream of the reaction chamber 14 through the riser 46. The mixture of gas and catalyst is accelerated in the narrower transport riser 46 and discharged from the primary catalyst separator 48 into the separation chamber 26. The primary catalyst separator 48 may be a riser termination device that utilizes horizontal, centripetal acceleration to separate the spent catalyst from the product gas. The arcuate conduit of the primary catalyst separator 48 directs the mixture of olefin product gas and spent catalyst to exit the riser 46 in a generally horizontal angular direction, accelerating centripetally, thereby causing the denser catalyst to move outwardly further than the less dense gas under the action of gravity. The catalyst loses angular momentum and falls into the lower catalyst bed 49 depicted by the upper boundary. The lighter gas rises in the separation chamber 26.

[0034] The separation chamber 26 may include a disengagement chamber 70 surrounding the upper end of the riser 46 and the primary separator 48. The vertical wall of the disengagement tank 70 is spaced apart from the shell of the separation chamber 26 of the reactor 12 to define an annular portion 72 located therebetween. The legs of the cyclone separators 50 and 52 may be located in the annular portion 72. The disengagement chamber 70 contains and confines the olefin product gas in a contained space, which may be defined by the vertical walls of the disengagement tank. At the same height, the volume of the contained space is less than the volume of the reactor 12, and specifically, less than the volume of the reaction chamber 26. The disengagement tank 70 is used to limit the travel of the product gas leaving the primary separator 48 at the reactor temperature so as to reduce the time of the product gas in the reactor 12, thereby mitigating the non-selective cracking reaction of the undesirable product.

[0035] The top of the disengagement drum 70 may be hemispherical or conical and feeds a gas recovery conduit 74 extending from the center of the top of the disengagement drum. The gas recovery conduit 74 is adjacent to the disengagement chamber 70. The gas recovery conduit 74 transports the olefin product gas to the distribution plenum 73. In order to minimize non-selective thermal cracking to a lower value of by-products, the product gas is quenched with a quench fluid from a distributor 80 fed by a pipeline 81 and a second distributor 82 fed by a pipeline 83 to cool the product gas to below the thermal cracking temperature. The quenching may be performed in the disengagement chamber 70 or in the gas recovery conduit 74. The first distributor 80 and the second distributor 82 may be located in the disengagement chamber 70 above the primary separator 48 but below the gas recovery conduit 74. The preferred design criteria is to perform the quenching downstream of the separation, so a smaller mass of material must be quenched.

[0036] The quench fluid is injected into the product stream from a first distributor 80 having a first end located at a first radial position from the axial center of the gas recovery conduit 74 and a second distributor 82 having a second end located at a second radial position from the axial center of the gas recovery conduit, the second radial position being different from the first radial position. The first end of the first distributor 80 may be at a higher elevation than the second end of the second distributor 82. The first distributor 80 and the second distributor 82 may have their ends located in the disengagement chamber 70 downstream of the primary separator 48 or in the gas recovery conduit 74.

[0037] Figure 1 The first distributor 80 and the second distributor 82 in the gas recovery conduit 74 have a horizontal configuration, but an upward or downwardly inclined configuration may also be suitable. The downwardly directed first distributor 80 and the downwardly directed second distributor 82 installed in the gas recovery conduit 74 or the disengagement chamber 70 can spray the quench fluid downward into the disengagement chamber 70.

[0038] A baffle 75 may be installed at the junction between the disengagement chamber 70 and the gas recovery conduit 74 to prevent and reduce swirl in the product gas stream centrifugally discharged from the primary separator 48. The baffle 75 should be located downstream of the primary separator 48.

[0039] The quenching fluid may contain a solvent and a recovered catalyst. The quenching fluid with the quenched product may pass through a primary cyclone 50 and a secondary cyclone 52. The molecular weight of the solvent may be heavier than the product with a lighter molecular weight. The solvent may be loaded with a lightly loaded catalyst comprising a slurry. The product gas is quenched with a solvent slurry so that the catalyst in the slurry is returned to the catalyst reserve in the reactor 12. The solvent may be an aromatic oil, such as comprising C9-C12 aromatic hydrocarbons.

[0040] Conduit 76 is directly conduited or connected between the distribution plenum 73 and the primary cyclone 50. The direct conduit from the disengaging chamber 70 to the primary cyclone 50 also prevents the product gas from escaping into the larger volume of the separation chamber 26, where excessive residence time may occur to allow non-selective thermal cracking. The deoxygenation catalyst separated from the olefin product gas by the primary catalyst separator 48 falls into the dense catalyst bed 49 in the separation chamber 26.

[0041] The cyclone separators 50, 52 may include a first cyclone separation stage and a second cyclone separation stage to further remove catalyst from the product gas. The olefin product gas is ducted to a plenum 54 from which the olefin product gas is discharged from the reactor 12 through a product outlet 56 in the product line. The superficial gas velocity in the transport riser 46 will be 12 m / s (40 ft / s) to 20 m / s (70 ft / s) and have a 64 kg / m 3 (4lb / ft 3 ) to 160kg / m 3 (10lb / ft 3 ) density, thereby constituting a dilute catalyst phase.

[0042] The catalyst separated from the product gas by the primary catalyst separator 48 falls into the dense catalyst bed 49. In one aspect, the primary cyclone separator 50 can collect the product gas from the gas recovery conduit 74 and transport the product gas separated from the catalyst to the secondary cyclone separator 52 to further separate the catalyst from the product gas, and then guide the secondary purified product gas to the plenum 54. The catalyst separated from the product gas in the cyclone separators 50, 52 is distributed through the dipleg into the dense catalyst bed 49. At this time, the catalyst separated in the separation chamber 26 is considered to be a spent catalyst because the deposits of coke are agglomerated thereon.

[0043] The regenerated portion of the spent catalyst collected in the dense bed 49 in the separation chamber 26 is transported to the catalyst regenerator 20 in the spent catalyst conduit 18 to burn the coke from the catalyst, thereby regenerating and heating the dehydrogenation catalyst. The vertical section of the spent catalyst conduit 18 may include a stripping section 60. A stripping gas such as steam or another inert gas may be fed into the lower end of the stripping section 60 to strip hydrocarbons from the spent catalyst entering the stripping section 60. A guide plate 62 may also be provided in the stripping section 60 to allow the spent catalyst to travel laterally in the stripping section, thereby exposing more catalyst particles to the upwardly flowing stripping gas. The guide plate 62 may be replaced with a packing and / or a grid (possibly with a downcomer) to promote contact between the catalyst and the stripping gas.

[0044] The recycle portion of the spent catalyst collected in the dense bed 49 of the separation chamber 26 enters the recycle catalyst conduit 34 through the inlet 35. The recycle portion of the spent catalyst is recycled in the recycle catalyst conduit 34 back to the first catalyst inlet 39 in the reaction chamber 14 of the reactor 12 as a first catalyst stream. The recycle portion of the spent catalyst is not regenerated before being returned to the reaction chamber 14.

[0045] The diplegs of cyclones 50, 52 respectively distribute spent dehydrogenation catalyst into dense dehydrogenation catalyst bed 49 in annulus 72. Openings in the lower section of the wall of disengaging chamber 70 allow catalyst confined in the disengaging chamber to move into annulus 72 and into recycle catalyst conduit 34 or regeneration conduit 18.

[0046] The first quench distributor 80 and the second quench distributor 82 can be connected to the gas recovery conduit 74 upstream in the separation chamber 70. The gas recovery conduit 74 is connected to the primary catalyst separator 48 downstream of the separation of the majority of the spent catalyst from the product gas. The spent catalyst bypasses the quench to retain heat in the catalyst. The product gas separated from the majority of the catalyst in the catalyst subjects a reduced amount of material to quenching, thereby requiring a smaller amount of quench fluid to achieve sufficient cooling to reduce the temperature of the product gas to below the thermal cracking temperature. The operation of the disengagement chamber 70 enables the accommodating and capturing of olefin product gas and catalyst with a greatly reduced mass. The gas recovery conduit 74 guides the olefin product gas from the disengagement chamber 70 to a narrow position to effectively expose it to the quench material injected into the gas recovery conduit. The quench material can be water or a hydrocarbon, such as an alkane recovered from a downstream dehydrogenation product recovery process.

[0047] The stripped spent dehydrogenation catalyst is transported to a regenerator 20 through a spent catalyst pipeline 18 to burn the coke on the spent catalyst and regenerate the spent catalyst into a regenerated catalyst. The catalyst regenerator 20 includes a combustion chamber 21 and a catalyst separator 23, which separates the regenerated catalyst from the flue gas when the flue gas generated in the combustion chamber 21 is discharged from the catalyst separator 23. An oxygen supply gas is provided to the combustion chamber 21 through a distributor 19, and the oxygen supply gas lifts the spent catalyst in the combustion chamber 21 through the catalyst separator 23 and enters the separation chamber 25. By contacting the oxygen supply gas under regeneration conditions, the coke is burned off from the spent catalyst. In an exemplary embodiment, air is used as an oxygen supply gas because air is easily available and provides enough oxygen for combustion. 10kg to 15kg of air is required for each kilogram of coke burned off from the spent catalyst. Exemplary regeneration conditions include temperatures from 500° C. (900° F.) to 900° C. (1700° F.) and pressures from 103 kPa (abs) (15 psia) to 450 kPa (abs) (70 psia) in the regenerator 20. A hydrocarbon fuel may be added to the regenerator 20, such as through the nozzle 28, to facilitate heat generated in the regenerator to drive the reaction in the reactor 12.

[0048] The regenerated catalyst is returned to the reactor 12 in the regenerated catalyst conduit 16. The regenerated catalyst conduit 16 has an inlet 17 connected to the regenerator 20 in the separation chamber 25, through which the regenerated catalyst from the regenerator is transported to the second catalyst inlet 43 in the reactor 12 as a second hotter catalyst stream. The regenerated catalyst is fed to the reactor 12 through the second catalyst inlet 43 which is the outlet of the regenerated catalyst conduit 16. The regenerated catalyst conduit 16 is connected to the second catalyst inlet 43.

[0049] Figure 2 is a partial cross-sectional plan view showing first and second distributors 80, 82 that deliver droplets across a larger cross-section of the gas recovery conduit 74 to provide an even distribution of quench fluid across the cross-section.

[0050] The first distributor 80 and the second distributor 82 are shown protruding through the wall 122 of the gas recovery conduit 74, which may be made of steel, and include an internal coating of a refractory lining 123. The first distributor 80 may include a first outer distributor barrel 124, which may be made of steel and coated with a refractory lining 125. The second distributor 82 may include a second distributor barrel 154, which may be made of steel and coated with a refractory lining 125. The first distributor 80 may include a first opening 130 for injecting hydrocarbon feed into the gas recovery conduit 74 or the disengagement chamber 70. The first distributor 80 may include a first cluster 126 of first openings 130 for injecting hydrocarbon feed into the gas recovery conduit 74 or the disengagement chamber 70. The first center 150 of the first opening 130 of the first distributor 130 or the first opening 130 of the first cluster 126 is located at a first radial position in the gas recovery conduit relative to the longitudinal center C in the gas recovery conduit 74. The first center 150 of the first distributor 130 is the geometric center of the first opening 130 in the case of only one first opening, or the geometric center of the first opening of the first cluster 126 in the case of the first distributor 80. The second distributor 82 may include a second opening 131 for injecting hydrocarbon feed into the gas recovery conduit 74 or the disengagement chamber 70. The second distributor 82 may include a second opening 131 of a second cluster 127 for injecting hydrocarbon feed into the gas recovery conduit 74 or the disengagement chamber 70. The second center 151 of the second opening 131 of the second distributor 131 or the second opening 131 of the second cluster 127 is located at a second radial position in the gas recovery conduit relative to the longitudinal center C in the gas recovery conduit 74. The second center 151 of the second distributor 131 is the geometric center of the second opening 131 in the case of only one second opening, or the geometric center of the second opening of the second cluster 127 in the case of the second distributor 82. The second radial position is different from the first radial position. The first radial position is further inward, further away from the wall 122, and closer to the center C than the second radial position because the first distributor 80 is longer than the second distributor 82 and extends farther into the gas recovery conduit 74. Alternatively, the first radial position can be at a different height than the second radial position. The first radial position can differ from the second radial position in height or in distance from the center C.

[0051] The first radial position may represent a first radius from the center of the container where the openings 131 of the first cluster 127 are located, and the second radial position may represent a second radius from the center of the container, which in this case is the gas recovery conduit 74, but it may be the disengagement chamber 70. The different radial positions may also be different in that they have different heights. Figure 1In , the radial positions vary in height and in radius from the center of the vessel. Figure 2 , the radial positions may be at the same height but have different radii from the center C of the gas recovery conduit 74.

[0052] The first opening 130 is an orifice in the first distributor 80 that emits the quenching fluid into the gas recovery conduit 74. The second opening 131 is an orifice in the second distributor 82 that emits the quenching fluid into the gas recovery conduit 74. The openings 130, 131 can be provided by small tubes 133, which give directions and patterns to the sprays of the quenching fluid from the corresponding openings. In addition, the openings 130, 131 themselves can be configured to give the desired trajectory to the sprays of the quenching fluid discharged therefrom. The openings 130, 131 in a specific cluster 126, 127 can be jointly configured to cooperatively spray feed in a desired pattern (such as in a fan-shaped pattern). The openings 130, 131 can be circular, such as annular or oval, or can include slots.

[0053] In one embodiment, the first opening 130 or the first opening 130 of the first cluster 126 can be located on the first end 132. In one embodiment, the second opening 131 or the second opening 131 of the second cluster 127 can be located on the second end 137. The ends 132, 137 and the tube 133 can be made of steel, or they can be made of ceramic material or coated to resist corrosion. The ends 132, 137 or the barrels 124, 154 can be removed from the distributor 80, 82, respectively, to replace new ends or barrels, respectively. The first end 132 can extend from the first distributor barrel 124. The second end 137 can extend from the second distributor barrel 154.

[0054] Figure 2 Depicted are ends 132, 137 of first openings 130 of a first cluster 126 and second openings 131 of a second cluster 127, respectively. The first openings 130 of the first cluster 126 at the first end 132 may be located on an inner end 136 of the first distributor 80. The inner end 136 of the first distributor 80 may protrude radially into the gas recovery conduit 74 to distribute droplets of quench fluid into the upwardly flowing product gas stream. The second openings 131 of the second cluster 127 at the second end 137 may be located on an inner end 136 of the second distributor 82. The inner end 136 of the second distributor 82 may protrude radially into the gas recovery conduit 74 to distribute droplets of quench fluid into the upwardly flowing product gas stream.

[0055] In one embodiment, the gas recovery conduit 74 may include a nozzle 135 for each distributor 80, 82. The nozzle 135 has a nozzle flange 139, which is bolted to the barrel flange 123 of the distributor barrel 124, 154. The distributor barrel 124, 154 receives an inert dispersion medium flow such as steam or nitrogen from a dispersion medium supply inlet 142 that is connected downstream to the dispersion medium supply device. The distributor barrel 124, 154 also receives a quench fluid such as an aromatic solvent by a quench fluid supply inlet 144 that is connected downstream to the quench fluid supply device. The dispersion medium travels in the first annular space 146 between the first internal quench pipe 148 and the distributor barrel 124. The first opening 130 of the first cluster 126 can be connected downstream to the quench supply inlet 144 and the medium supply inlet 142. Similarly, in the second distributor 82, the dispersion medium travels in the second annular space 147 between the second internal quench pipe 149 and the second distributor barrel 154. The first openings 130 of the first cluster 126 and the second openings 131 of the second cluster 127 may be in downstream communication with a respective quench supply inlet 144 and a respective medium supply inlet 142 .

[0056] In the first distributor 80, the terminal conduit 138 extends from the first quench tube 148 to the first end 132 and transports the mixture of quench fluids from the internal quench tube 148 to the first opening 130 of the first cluster 126 at the first end 132. In the second distributor 82, the terminal conduit 138 extends from the second internal quench tube 149 to the second end 137 and transports the mixture of quench fluids from the second internal quench tube 149 to the second opening 131 of the second cluster 127 at the terminal head 137. The quench flow may pass from the first internal quench tube 148 through vanes that may be in the terminal conduit 138, thereby causing the quench fluid to swirl before mixing with the dispersion medium that enters from the annular space 146 through the port 134 in the first end 132 and exits through the opening 130 in the terminal cluster 126 at the first end 132. The quench flow may pass from the second internal quench conduit 149 through vanes that may be in the terminal conduit 138, causing the quench fluid to swirl before mixing with the dispersion medium that enters from the annular space 147 through the port 134 in the second terminal 137 and exits through the second openings 131 in the second cluster 127 on the second terminal 137. Several ports 134 may be utilized and located at various locations. The dispersion gas is mixed with the quench liquid in the distributor 80, 82, atomizing the quench liquid sprayed from the distributor.

[0057] The first distributor 80 injects quench fluid into the product gas stream through a first opening 130 centered at a first radial position, and the second distributor 82 injects quench fluid through a second opening 131 centered at a second radial position different from the first radial position.

[0058] Figure 3 The center 150, 151 of the dispenser 80, 82 of a cluster of openings 130, 131 located on the dispenser tip 132, 137, respectively, is shown. For example, the openings 130, 131 define an elliptical cluster on the dispenser tip 132, 137, respectively, which defines the geometric center 150, 151. If only one opening 130, 131 is provided on the dispenser tip 132, 137 of the dispenser 80, 82, the center 150, 151 would be the geometric center of the single opening 130, 131.

[0059] Figure 4 Shown in Figure 1 3-3 in FIG. 1 and 1 , showing a plan cross-sectional view of the reactor 12 showing the separation vessel 26, the disengagement chamber 70 and the gas recovery conduit 74. The first set or plurality 84 of first quench distributors 80 direct the quench fluid from the first opening 130 ( Figure 2 ) is injected into the product gas flow, and the center of the first opening is located at a first radial position on the imaginary circle R1. The center 150 of the first group 84 of first distributors 80 is located at Figure 3 The second group or plurality of second quench distributors 82 direct the quench fluid from the second opening 131 ( Figure 2 ) is injected into the product gas flow, and the center 151 of the second opening is located at a second radial position on the imaginary circle R2, and the second radial position is different from the first radial position located on the first imaginary circle R1. The first radial position defines the first imaginary circle R1, and the second radial position defines the second imaginary circle R2. The second group 86 second distributor 82 is located Figure 3 1 o'clock, 2 o'clock, 4 o'clock, 5 o'clock, 7 o'clock, 8 o'clock, 10 o'clock and 11 o'clock positions in the embodiment of the present invention. Both imaginary circles R1 and R2 are centered on the center C. The circles R1 and R2 can have different radii from the center C. The two imaginary circles R1 and R2 can also be arranged at the same radial distance from the center C and at different heights, or at different radial distances from the center and at different heights. The first radial position represented by the circle R1 can be different from the second radial position represented by the circle R2 in height or in distance from the center C.

[0060] The quench fluid from the first quench fluid conduit 90 is supplied to the first arcuate manifold 91 which supplies the quench fluid supply inlets 144 ( Figure 2 The quench fluid from the second quench fluid conduit 92 is supplied to the second arcuate manifold 93 which supplies the quench fluid supply inlets 144 of all the second distributors 82 in the second set 86 of second quench distributors ( Figure 2 ).

[0061] The dispersion medium from the first dispersion medium conduit 94 is supplied to the third arc-shaped manifold 95, which supplies the dispersion medium supply inlets 142 ( Figure 2 The dispersion medium from the second quench fluid conduit 96 is supplied to the second arcuate manifold 97 which supplies the quench fluid supply inlets 142 of all the second distributors 82 in the second set 86 of second quench distributors ( Figure 2 ).

[0062] The first set 84 of 2 to 16 first distributors (of which 4 are shown as first openings 130 ( Figure 2 ) spraying atomized quench fluid) and a second set 86 of 4 to 20 second distributors (8 of which are shown as being from a second opening 131 ( Figure 2 The arrangement of spraying atomized quench fluid distributes the quench fluid over a more complete cross-section of the gas recovery conduit 74 to ensure more rapid and complete quenching of the product gas that may be separated from a large portion of the catalyst by centripetal separation.

[0063] Specific implementation plan

[0064] While the following is described in conjunction with specific embodiments, it should be understood that this description is intended to illustrate and not to limit the scope of the foregoing description and the appended claims.

[0065] A first embodiment of the present invention is a method of distributing a quenching fluid into a product stream, comprising contacting a feed stream with a catalyst stream to convert the feed stream into a product; and spraying the quenching fluid from a first distributor through at least one first opening and from a second distributor through at least one second opening into the product stream, the at least one first opening having a first center located at a first radial position, the at least one second opening having a second center located at a second radial position different from the first radial position. An embodiment of the present invention is one, any one, or all of the first embodiment in this paragraph to the previous embodiments in this paragraph, and further comprises mixing a gas with a quenching liquid in the first distributor to atomize the quenching liquid sprayed from the first distributor. An embodiment of the present invention is one, any one, or all of the first embodiment in this paragraph to the previous embodiments in this paragraph, and further comprises spraying a quenching fluid into the product stream after separating the catalyst from the product stream. One embodiment of the present invention is one, any or all of the first embodiment in this paragraph to the previous embodiments in this paragraph, and also includes spraying the quenching fluid from the first distributor through the first opening and from the second distributor through the second opening into the product stream, the first opening having a first center located at a first radial position, and the second opening having a second center located at a second radial position different from the first radial position. One embodiment of the present invention is one, any or all of the first embodiment in this paragraph to the previous embodiments in this paragraph, and also includes separating the product stream from the catalyst stream by centripetal acceleration. One embodiment of the present invention is one, any or all of the first embodiment in this paragraph to the previous embodiments in this paragraph, and also includes preventing the product stream from swirling upstream of the quenching. One embodiment of the present invention is one, any or all of the first embodiment in this paragraph to the previous embodiments in this paragraph, wherein the quenching fluid contains a catalyst discharged from the reactor as a liquid. One embodiment of the present invention is one, any or all of the first embodiment in this paragraph to the previous embodiments in this paragraph, wherein the catalyst in the quenching fluid is returned to the catalyst storage in the reactor. One embodiment of the present invention is one, any or all of the first embodiment in this paragraph to the previous embodiments in this paragraph, and also includes spraying the quenching fluid from the first distributor in a horizontal trajectory. One embodiment of the present invention is one, any or all of the first embodiment in this paragraph to the previous embodiments in this paragraph, and also includes a plurality of first distributors having first openings and a plurality of second distributors having second openings, the first openings having a first center located at a first radial position defining a first imaginary circle, and the second openings having a second center located at a second radial position defining a second imaginary circle different from the first imaginary circle.An embodiment of the present invention is one, any or all of the first embodiment in this paragraph to the previous embodiments in this paragraph, wherein the first distributor is located at a height higher than the second distributor.

[0066] A second embodiment of the present invention is a method for distributing a quenching fluid into a product stream, comprising contacting a feed stream with a catalyst stream to convert the feed stream into a product; mixing a gas with a quenching liquid in a first distributor to atomize the quenching liquid; and spraying the quenching fluid from the first distributor into the product stream. One embodiment of the present invention is one, any or all of the second embodiment in this paragraph to the previous embodiments in this paragraph, and also includes spraying a quenching fluid from the first distributor through at least one first opening centered on a first radial position and from the second distributor through at least one second opening centered on a second radial position different from the first radial position. One embodiment of the present invention is one, any or all of the second embodiment in this paragraph to the previous embodiments in this paragraph, and also includes separating the product stream from the catalyst stream by centripetal acceleration. One embodiment of the present invention is one, any or all of the second embodiment in this paragraph to the previous embodiments in this paragraph, wherein the quenching fluid comprises a catalyst discharged from the reactor as a liquid. One embodiment of the present invention is one, any or all of the second embodiment in this paragraph to the previous embodiments in this paragraph, wherein the catalyst in the quenching fluid is returned to the catalyst inventory in the reactor. One embodiment of the present invention is one, any or all of the second embodiment in this paragraph to the previous embodiments in this paragraph, further comprising spraying the quenching fluid from the first distributor in a horizontal trajectory. One embodiment of the present invention is one, any or all of the second embodiment in this paragraph to the previous embodiments in this paragraph, further comprising a plurality of first distributors having first openings centered at a first radial position and a plurality of second distributors having second openings centered at a second radial position.

[0067] The third embodiment of the present invention is a method of distributing a quenching fluid into a product stream, comprising contacting a feed stream with a catalyst stream to convert the feed stream into a product; and spraying the quenching fluid from a first group of first distributors through a first opening and from a second group of second distributors through a second opening into the product stream, the first opening having a first center located at a first radial position, and the second opening having a second center located at a second radial position different from the first radial position. One embodiment of the present invention is one, any one, or all of the third embodiment in this paragraph to the previous embodiments in this paragraph, and further comprises spraying the quenching fluid into the product stream after separating the catalyst from the product stream. One embodiment of the present invention is one, any one, or all of the third embodiment in this paragraph to the previous embodiments in this paragraph, and further comprises separating the product stream from the catalyst stream by centripetal acceleration.

[0068] Although there is no further detailed description, it is believed that those skilled in the art can utilize the present invention to the greatest extent by using the foregoing description and can easily determine the essential characteristics of the present invention without departing from the spirit and scope of the present invention to make various changes and modifications of the present invention and adapt it to various usages and conditions. Therefore, the aforementioned preferred specific embodiments should be understood as merely illustrative and not to limit the rest of the present disclosure in any way, and are intended to cover various modifications and equivalent arrangements included within the scope of the appended claims.

[0069] In the foregoing, all temperatures are set forth in degrees Celsius and all parts and percentages are by weight unless otherwise indicated.

Claims

1. A method of distributing a quench fluid into a product stream, comprising: contacting a feed stream with a catalyst stream to convert the feed stream into a product; as well as The quenching fluid is injected into the product stream from a first distributor through at least one first opening and from a second distributor through at least one second opening, wherein the at least one first opening has a first center located at a first radial position and the at least one second opening has a second center located at a second radial position different from the first radial position. 2 . The method of claim 1 , further comprising mixing a gas with the quench liquid in a first distributor to atomize the quench liquid sprayed from the first distributor.

3. The method of claim 1 further comprising injecting a quenching fluid into the product stream after separating the catalyst from the product stream.

4. The method according to claim 1 also includes injecting the quenching fluid from a first distributor through a first opening and from a second distributor through a second opening into the product stream, wherein the first opening has the first center located at a first radial position and the second opening has the second center located at a second radial position different from the first radial position.

5. The method of claim 4, further comprising preventing the product stream from swirling upstream of quenching.

6. The process of claim 3 wherein the quench fluid comprises catalyst discharged from the reactor as a liquid.

7. The method of claim 4, wherein the catalyst in the quench fluid is returned to the catalyst inventory in the reactor.

8. The method of claim 3, further comprising spraying the quench fluid from the first distributor in a horizontal trajectory.

9. The method according to claim 1 further includes a plurality of first distributors having a first opening and a plurality of second distributors having a second opening, wherein the first opening has a first center located at a first radial position defining a first imaginary circle, and the second opening has a second center located at a second radial position defining a second imaginary circle different from the first imaginary circle.

10. The method according to claim 1, wherein the first dispenser is located at a height higher than that of the second dispenser.

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