Particulate solid dispenser suitable for dispensing

Abstract

A particulate solids dispenser suitable for dispensing two flows of particulate solids may include an inner conduit extending from an inner conduit inlet to an inner conduit outlet. The inner conduit may be at least partially defined by an inner wall, and the inner wall may be disposed about a central axis. The particulate solids dispenser may also include an outer conduit at least partially defined by the inner wall and the outer wall. The outer conduit may extend from an outer conduit inlet to an outer conduit outlet. The outer wall may be disposed about the central axis, and a cross-section of the outer wall may surround a cross-section of the inner wall in a plane perpendicular to the central axis. The particulate solids dispenser may also include a first solids guide positioned above the central axis and downstream of the inner conduit outlet. The particulate solids dispenser may also include a second solids guide attached to the inner wall and extending radially outward from the central axis. The inner conduit may extend through the outer conduit such that the inner conduit outlet may be downstream of the outer conduit outlet.

Description

[0001] Cross - Reference to Related Applications

[0002] This application claims the benefit of U.S. Provisional Application Serial No. 63 / 428,524, filed on November 29, 2022, the entire disclosure of which is hereby incorporated by reference herein. Technical Field

[0003] The embodiments described herein generally relate to dispensers, and more particularly to dispensers suitable for dispensing a granular solid stream. Background Art

[0004] Granular solids can be utilized in chemical processes in a variety of ways. For example, granular solids can be used as catalysts in chemical processes such as fluidized - bed reactions. Since the requirements for various chemical processes can vary widely, introducing granular solids in a particular manner may benefit the chemical process. Thus, there is a need in the industry for granular solid dispensers that can dispense granular solids to meet the process requirements. Summary of the Invention

[0005] Chemical processes can utilize granular solids, and in some cases, multiple separate granular solid streams injected into the same reactor or other vessel. Granular solid dispensers are described herein that are suitable for dispensing two separate granular solid streams into different parts of a reactor or other processing unit. For example, some embodiments described herein can be suitable for causing two different granular solid streams to be delivered at different heights. Such dispensers can be operative to deliver solids (such as catalysts) into a fluidized - bed reactor, etc., where in some embodiments, such catalyst flow patterns may be beneficial. The dispensers described herein may be capable of introducing multiple granular solid streams at different heights, but where both of these streams emanate from near or at the center of the reactor or other processing vessel.

[0006] According to one or more embodiments described herein, a granular solid dispenser adapted to dispense two streams of granular solids may include an inner conduit that extends from an inner conduit inlet to an inner conduit outlet. The inner conduit may be at least partially defined by an inner wall, and the inner wall may be arranged about a central axis. The granular solid dispenser may further include an outer conduit that is at least partially defined by the inner wall and an outer wall. The outer conduit may extend from an outer conduit inlet to an outer conduit outlet. The outer wall may be arranged about the central axis, and a cross-section of the outer wall may enclose a cross-section of the inner wall in a plane perpendicular to the central axis. The granular solid dispenser may further include a first solid guide positioned above the central axis and downstream of the inner conduit outlet. The granular solid dispenser may further include a second solid guide attached to the inner wall and extending radially outward from the central axis. The inner conduit may extend through the outer conduit such that the inner conduit outlet may be located downstream of the outer conduit outlet.

[0007] According to one or more embodiments, a granular solid dispenser adapted to dispense two streams of granular solids may include an inner conduit that extends from an inner conduit inlet to an inner conduit outlet. The inner conduit may be at least partially defined by an inner wall, and the inner wall may be arranged about a central axis. The granular solid dispenser may further include an outer conduit that is at least partially defined by the inner wall and an outer wall. The outer conduit may extend from an outer conduit inlet to an outer conduit outlet. The outer wall may be arranged about the central axis. A cross-section of the outer wall may enclose a cross-section of the inner wall in a plane perpendicular to the central axis. The granular solid dispenser may further include an inlet conduit that is at least partially defined by an inlet conduit wall. The inlet conduit may extend from an inlet conduit inlet to an inlet conduit outlet. The inlet conduit may intersect the outer wall. The inlet conduit outlet may be positioned at the inner wall such that the inlet conduit may communicate with the inner conduit. The granular solid dispenser may further include a first solid guide positioned above the central axis and downstream of the inner conduit outlet. The granular solid dispenser may further include a second solid guide attached to the inner wall and extending radially outward from the central axis. The inner conduit may extend through the outer conduit such that the inner conduit outlet may be located downstream of the outer conduit outlet.

[0008] According to one or more embodiments, a granular solid dispenser for dispensing two streams of granular solids may include an inner conduit extending from an inner conduit inlet to an inner conduit outlet. The inner conduit may be at least partially defined by an inner wall. The inner wall may be arranged about a central axis. The granular solid dispenser may further include an outer conduit at least partially defined by the inner wall and an outer wall. The outer conduit may extend from an outer conduit inlet to an outer conduit outlet. The outer wall may be arranged about the central axis. A cross-section of the outer wall may enclose a cross-section of the inner wall in a plane perpendicular to the central axis. The granular solid dispenser may further include an inlet conduit at least partially defined by an inlet conduit wall. The inlet conduit may extend from an inlet conduit inlet to an inlet conduit outlet. The inlet conduit outlet may be positioned at the outer wall such that the inlet conduit may communicate with the outer conduit. The granular solid dispenser may further include a first solid guide positioned above the central axis and downstream of the inner conduit outlet. The granular solid guide may further include a second solid guide attached to the inner wall and extending radially outward from the central axis. The inner conduit may extend through the outer conduit such that the inner conduit outlet may be located downstream of the outer conduit outlet.

[0009] Additional features and advantages of the present disclosure will be set forth in the detailed description which follows, and in part will be obvious from the description, or may be learned by practice of the embodiments described herein, including the detailed description which follows, the claims, as well as the drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0010] The embodiments set forth in the drawings are illustrative and exemplary in nature and are not intended to limit the subject matter defined by the claims. The following detailed description of illustrative embodiments can be understood when read in conjunction with the following drawings, in which like reference numerals indicate like structures and in which:

[0011] Figure 1 A granular solid dispenser is schematically depicted in accordance with one or more embodiments disclosed herein;

[0012] Figure 2 Another granular solid dispenser is schematically depicted in accordance with one or more embodiments disclosed herein;

[0013] Figure 3 A chemical processing vessel using a granular solid dispenser is schematically depicted in accordance with one or more embodiments disclosed herein; and Figure 1

[0014] Figure 4Schematically depicts a reactor system that can be used in conjunction with embodiments of the present disclosure in accordance with one or more embodiments disclosed herein.

[0015] Additional features and advantages of the present disclosure will be set forth in the detailed description below, and will in part be apparent to those of ordinary skill in the art from the description, or can be learned by practice of the embodiments described herein, including the detailed description below, the claims, and the drawings.

[0016] It should be understood that both the foregoing general description and the following detailed description describe various embodiments and are intended to provide an overview or framework for understanding the nature and characteristics of the claimed subject matter. The drawings are included to provide a further understanding of the various embodiments, and the drawings are incorporated in and constitute a part of this specification. The drawings illustrate the various embodiments described herein and, together with the description, explain the principles and operation of the claimed subject matter. Detailed Description

[0017] Reference will now be made specifically to various embodiments of apparatus, components, and methods, examples of which are illustrated in the drawings. Wherever possible, the same reference numbers will be used throughout the drawings to refer to the same or like parts.

[0018] The present disclosure generally relates to granular solid dispensers and the operation of such granular solid dispensers. Referring to Figure 1 and Figure 2 , perspective schematic views of two granular solid dispensers 100 are depicted. Figure 1 and Figure 2 Each of the embodiments of Figure 1 and Figure 2 includes an inner conduit 200 and an outer conduit 300, respectively. Generally speaking, Figure 1 and Figure 2 the granular solid dispensers 100 are similar in many respects but also include some differences, as described. Specifically, Figure 1 the solid dispenser of Figure 2 includes an inlet conduit 270 that is in fluid communication with the inner conduit 200, while Figure 2 the embodiment of

[0019] Still referring to Figure 1 and Figure 2, the particulate solid dispenser 100 may include an inner conduit 200 and an outer conduit 300. The inner conduit 200 may extend from an inner conduit inlet 210 to an inner conduit outlet 252. The inner conduit 200 may be at least partially defined by an inner wall 260. Generally speaking, the inner conduit 200 may be bounded by the inner wall 260, which may be, for example, a tubular member. The inner wall 260 may be arranged around a central axis 600. The outer conduit 300 may extend from an outer conduit inlet 310 to an outer conduit outlet 352. The outer conduit 300 may be at least partially defined by the inner wall 260 and an outer wall 360, wherein the space between the inner wall 260 and the outer wall 360 may define the outer conduit 300. The outer wall 360 may be arranged around the central axis 600, and the cross-section of the outer wall 360 may enclose the cross-section of the inner wall 260 in a plane perpendicular to the central axis 600. As described herein, generally speaking, a first particulate solid stream may be passed upward through the inner conduit 200, and a second particulate solid stream may be passed upward through the outer conduit 300.

[0020] In one or more embodiments, the inner wall 260 may have a cross-sectional shape that is circular, oval, elliptical, or polygonal in a plane perpendicular to the central axis 600. In one or more embodiments, the outer wall 360 may have a cross-sectional shape that is circular, oval, elliptical, or polygonal in a plane perpendicular to the central axis 600. In some embodiments, both the inner wall 260 and the outer wall 360 may have a circular cross-sectional shape in a plane perpendicular to the central axis 600, as Figure 1 and Figure 2 depicted. In one or more embodiments, the inner wall 260 and the outer wall 360 may have the same cross-sectional shape in a plane perpendicular to the central axis 600. In other embodiments, the inner wall 260 and the outer wall 360 may have different cross-sectional shapes in a plane perpendicular to the central axis 600. In some embodiments, as Figure 1 and Figure 2 depicted, the outer wall 360 may have a refractory lining 370. In some embodiments ( Figure 1 and 2 not shown), the outer wall 360 may not have a refractory lining 370.

[0021] As described with respect to Figure 1 and Figure 2 , the inner conduit 200 and the outer conduit 300 may form a coaxial arrangement. In such embodiments, the inner conduit 200 may be surrounded by the outer conduit 300 in a direction perpendicular to the central axis 600.

[0022] In one or more embodiments, the inner conduit 200 extends through the outer conduit 300. In such embodiments, the inner conduit outlet 252 may be located downstream of the outer conduit outlet 352. For example, as Figure 1 and Figure 2As depicted, the inner wall 260 (defining the inner conduit 200) extends upwardly past the end of the outer wall 360 (defining the outer conduit outlet 352 of the outer conduit 300). As used in the present disclosure, the term "downstream" refers to a position along the conduit that is closer to the outlet than the inlet, typically in the direction of the granular solid flow. As used in the present disclosure, the term "upstream" refers to a position along the conduit that is closer to the inlet than the outlet, typically in the opposite direction of the granular solid flow.

[0023] As described herein, generally, a first granular solid flow may pass above a second granular solid flow and be delivered from the inner conduit 200 through the inner conduit outlet 252, and the second granular solid flow may be delivered from the outer conduit 300 through the outer conduit outlet 352. In some embodiments, the portion of the inner wall 260 that extends upwardly past the end of the outer wall 360 (defining the outer conduit outlet 352 of the outer conduit 300) may have a refractory lining on the side of the inner wall 260 opposite the inner conduit 200.

[0024] The granular solid dispenser 100 may include a first solid guide 240 and a second solid guide 340. The first solid guide may be positioned above the central axis 600 and downstream of the inner conduit outlet 252 such that granular solids may flow from the inner conduit inlet 210 to the inner conduit outlet 252 and be guided out of the granular solid dispenser by the first solid guide 240. In one or more embodiments, as Figure 1 and Figure 2 shown, the first solid guide 240 may be a first deflector plate. Generally, as described herein, a first granular solid flow may be delivered from the inner conduit outlet 252 and contact the first deflector plate. Then, the first granular solid flow may be deflected radially outward from the granular solid dispenser 100 by the first deflector plate. The first solid guide 240 may be supported in a variety of ways, such as being attached to the inner wall 260 etc. (not depicted in the figures).

[0025] In one or more embodiments, the second solid guide 340 may be attached to the inner wall 260 and extend radially outward from the central axis 600. In one or more embodiments, the second solid guide 340 may be positioned on a portion of the inner wall 260 that extends past the outer wall 360. In some embodiments, as Figure 1 and Figure 2 shown, the second solid guide 340 and the inner wall 260 may form a coaxial arrangement. In such embodiments, a portion of the inner wall 260 may be surrounded by the second solid guide 340. In some embodiments, the inner wall 260 may extend past the second solid guide 340. For example, as Figure 1 and Figure 2 shown, a portion of the inner wall 260 extends upwardly past the second solid guide 340. In Figure 1 andFigure 2 In some embodiments not shown, the inner wall 260 may not extend past the second solid guide 340. In such embodiments, the portion of the inner wall 260 that defines the inner duct outlet 252 of the inner duct 200 may be flush with the surface of the second solid guide 340. In one or more embodiments, as Figure 1 and Figure 2 shown, the second solid guide 340 may be a second deflector plate. Generally speaking, as described herein, the second particulate solid stream may be delivered out of the outer duct outlet 352 and contact the second deflector plate 340. Then, the second particulate solid stream may be deflected radially outward from the particulate solid dispenser 100 by the second deflector plate.

[0026] In one or more embodiments, when the first solid guide 240 is circular, the area of a cylinder having a radius equal to the radius of the first solid guide 240 and a height equal to the distance between the first solid guide 240 and the inner duct outlet 252 may be 125% to 175% of the cross-sectional area of the inner wall 260. For example, the area of the cylinder may be 125% to 170% of the cross-sectional area of the inner duct outlet 252, such as 125% to 165%, 125% to 160%, 125% to 155%, 125% to 150%, 125% to 145%, 125% to 140%, 125% to 135%, 125% to 130%, 130% to 175%, 130% to 170%, 130% to 165%, 130% to 160%, 130% to 155%, 130% to 145%, 130% to 140%, 130% to 135%, 135% to 175%, 135% to 170%, 135% to 165%, 135% to 160%, 135% to 155%, 135% to 150%, 135% to 145%, 135% to 140%, 140% to 175%, 140% to 170%, 140% to 165%, 140% to 160%, 140% to 155%, 140% to 150%, 140% to 145%, 145% to 175%, 145% to 170%, 145% to 165%, 145% to 160%, 145% to 155%, 145% to 150%, 150% to 175%, 150% to 170%, 150% to 165%, 150% to 160%, 150% to 155%, 155% to 175%, 155% to 170%, 155% to 165%, 155% to 160%, 160% to 175%, 160% to 170%, 160% to 165%, 165% to 175%, 165% to 170%, or 170% to 175%. Such a ratio may allow the particulate solid to enter the container well.

[0027] In other embodiments, one or both of the first solid guide 240 and the second solid guide 340 may be a tube dispenser as disclosed in U.S. Patent No. 9,360,759, which is incorporated herein by reference in its entirety.

[0028] In some embodiments, as Figure 1 and Figure 2 shown, the granular solid dispenser 100 may include an inlet conduit 270. The inlet conduit 270 may be at least partially defined by an inlet conduit wall 274. The inlet conduit 270 may extend from an inlet conduit inlet 275 to an inlet conduit outlet 272. Generally speaking, the inlet conduit 270 may be bounded by the inlet conduit wall 274, which may be, for example, a tubular member. The inlet conduit wall 274 may be arranged around a central inlet conduit axis. In one or more embodiments, the inlet conduit wall 274 may have a circular, oval, elliptical, or polygonal cross-sectional shape in a plane perpendicular to the central inlet conduit axis. In one or more embodiments, a refractory lining 370 may cover at least a portion of the inlet conduit wall 274. In Figure 1 and Figure 2 some embodiments not shown, the refractory lining 370 may not cover at least a portion of the inlet conduit wall 274.

[0029] Now referring to Figure 1 , in one or more embodiments, the inlet conduit 270 may intersect the outer wall 360. In one or more embodiments, the inlet conduit 270 may be positioned at the inner wall such that the inlet conduit 270 communicates with the inner conduit 200. In such embodiments, the inlet conduit outlet 272 may be the inner conduit inlet 210. Generally speaking, as described herein, a first granular solid stream may pass through the inlet conduit 270 and enter the inner conduit 200. In some embodiments, as Figure 1 depicted, the inlet conduit 270 may engage the inner conduit 200 at an angle such that the inlet conduit outlet 272 points in a generally upstream direction of the inner conduit 200. In other embodiments, the inlet conduit 270 may engage the inner conduit 200 at an angle such that the inlet conduit outlet 272 points in a generally downstream direction of the inner conduit 200 ( Figure 1 not depicted).

[0030] Now referring to Figure 2 , in one or more embodiments, the inlet conduit 270 may be positioned at the outer wall such that the inlet conduit 270 communicates with the outer conduit. In such embodiments, the inner conduit outlet 272 may be the outer conduit inlet 310. Generally speaking, as described herein, a second granular solid stream may pass through the inlet conduit 270 and enter the outer conduit 300. In such embodiments, the inlet conduit outlet 272 may be the outer conduit inlet 310. In some embodiments, asFigure 2 As depicted in Figure 2 , the inlet conduit 270 may engage the outer conduit 300 at an angle such that the inlet conduit outlet 272 is directed generally upstream of the outer conduit 300. In other embodiments, the inlet conduit 270 may engage the outer conduit 300 at an angle such that the inlet conduit outlet 272 is directed generally downstream of the outer conduit 300 ( Figure 2 not depicted in Figure 2 ).

[0031] Returning to Figure 1 , in one or more embodiments, the particulate solid dispenser 100 may include a particulate solid director 500. Generally speaking, as described herein, the particulate solid director 500 may similarly direct a second stream of particulate solids through the outer conduit inlet 310 around the inner wall 260 and through the outer conduit 300 into the outer conduit 300. In one or more embodiments, the particulate solid director 500 may be at least partially defined by the inner conduit wall 260. Generally speaking, the diameters of the particulate solid director 500 in combination with the inner wall 260 and the outer wall 360 may be oriented such that the cross-sectional area of the outer conduit 300 is generally equal to or at least within the tolerance of the height of the outer conduit 300. As will be understood by those skilled in the art, this aspect may maintain the fluidization and apparent velocity of the solids throughout the height of the outer conduit 300.

[0032] Now referring to Figure 3 , a chemical processing vessel 400 utilizing the Figure 1 particulate solid dispenser 100 is schematically depicted. Although Figure 3 not depicted in Figure 3 , the Figure 2 particulate solid dispenser 100 may also be used in the chemical processing vessel 400. The chemical processing vessel 400 may include a vessel wall 410, a feed inlet 434, a feed distribution plate 450, and a processed chemical outlet 440. The feed inlet 434 may be at least partially defined by the vessel wall 410. In one or more embodiments, the particulate solid dispenser 100 may extend into the chemical processing vessel 400 such that the inner conduit outlet 252 may be downstream of the outer conduit outlet 352 relative to the feed inlet 434 (at the bottom of the vessel 400). In some embodiments, the particulate solid dispenser 100 may extend into the chemical processing vessel through the bottom end of the chemical processing vessel, as Figure 3 depicted in Figure 3 .

[0033] In one or more embodiments, the chemical processing vessel 400 may include a feed distribution plate 450. The feed distribution plate 450 may evenly distribute the feed from the feed inlet 434 over the entire surface of the feed distribution plate 450. In embodiments where the chemical processing vessel 400 includes a feed distribution plate 450, the granular solid dispenser 100 may be different from the feed distribution plate 450. For example, the outer wall 360 and the feed distribution plate 450 may be spaced apart such that the granular solid dispenser 100 and the feed distribution plate 450 do not engage and / or are not connected. In some embodiments where the chemical processing vessel 400 includes a feed distribution plate 450, the outer conduit outlet 352 may be positioned between the inner conduit outlet 252 and the feed distribution plate 450. In some embodiments, in the case where the chemical processing vessel 400 includes a feed distribution plate 450, the feed distribution plate 450 may be between the inner conduit outlet 252 and the outer conduit outlet 352 ( Figure 3 not depicted). In one or more embodiments, the chemical processing vessel 400 may be suitable for use as a fast fluidized bed, turbulent bed, or bubbling bed reactor.

[0034] The operation of the chemical processing vessel 400 including the granular solid dispenser 100 will now be described in the context of Figure 3 . The chemical processing vessel 400 may be operated by first passing a feed stream through the feed inlet 434 into the chemical processing vessel 400. In embodiments where the chemical processing vessel includes a feed distribution plate 450, the feed stream may then pass through the feed distribution plate. The feed stream generally travels upward through the chemical processing vessel from the feed inlet 434 to the treated chemical outlet 440. A first granular solid stream may pass through the inlet conduit 270 and enter the inner conduit 200 through the inlet conduit outlet 272, and a second granular solid stream may enter the outer conduit 300 separately through the outer conduit inlet 310. The two granular solid streams may be passed upward through the inner and outer conduits to the chemical processing vessel 400. The second granular solid stream may leave the outer conduit 300 through the outer conduit outlet 352. The second granular solid stream may then contact the second solid guide 340 and be directed out of the granular solid dispenser 100 and into the chemical processing vessel 400. The first granular solid stream may leave the inner conduit 200 through the inner conduit 252. The first granular solid stream may then contact the first solid guide 240 and be directed out of the granular solid dispenser 100 and into the chemical processing vessel 400. As Figure 3 shown, when the second granular solid stream enters the chemical processing vessel below the first granular solid stream, the feed traveling from the feed inlet 434 toward the treated chemical outlet 440 will contact the second granular solid stream directed into the chemical processing vessel by the second solid guide 340 before the first granular solid stream directed into the chemical processing vessel by the first solid guide 240.

[0035] In a chemical processing vessel 400, a feed stream and two granular solid streams may be mixed to form a mixed stream. The mixed stream may be transferred out of the chemical processing vessel 400 through a treated chemical outlet 440.

[0036] In one or more embodiments, the granular solids in the granular solid streams may be capable of fluidizing. In some embodiments, the granular solids may exhibit characteristics known in the industry as "Geldart A" or "Geldart B" characteristics. According to D. Geldart, Gas Fluidization Technology, John Wiley & Sons (New York, 1986), pages 34-37; and D. Geldart, "Types of Gas Fluidization", Powder Technol. 7 (1973) 285-292, which are hereby incorporated by reference in their entirety, the particles may be classified as "Group A" or "Group B".

[0037] Group A is understood by those skilled in the art to represent aeratable powders, having a fluidization with a range without bubbles; high bed expansion; slow and linear degassing rate; bubble characteristics, which may include the advantage of splitting / reattaching bubbles, having a maximum bubble size and a large wake; a high level of solid mixing and gas backmixing, assuming U - umf is equal (U is the velocity of the carrier gas, and Umf is the minimum fluidization velocity, typically but not necessarily measured in meters per second (m / s), i.e., there is an excessive gas velocity); axisymmetric slug characteristics; and no spouting except in very shallow beds. The listed characteristics tend to improve as the average particle size decreases, assuming cfp is equal; or as the proportion of <45 micrometers (μm) increases; or as the pressure, temperature, viscosity, and density of the gas increase. Generally, the particles may exhibit a small average particle size and / or a low particle density (<1.4 grams per cubic centimeter, g / cm 3 ); are easily fluidized, with smooth fluidization at low gas velocities; and may exhibit controlled bubbling with small bubbles at higher gas velocities.

[0038] Group B is understood by those skilled in the art to represent "sand-like" powders, which start to bubble at Umf; exhibit moderate bed expansion; rapid degassing; no limitation on bubble size; a moderate level of solid mixing and gas backmixing, assuming U - umf is equal; both axisymmetric and asymmetric slugs; and spouting only in shallow beds. These characteristics tend to improve as the average particle size decreases, but the particle size distribution and a certain uncertainty of the gas, pressure, temperature, viscosity, or density seem to have little effect on improving these characteristics. Generally, when the density (pp) is 1.4 < pp < 4 g / cm3 When, the particle size (cfp) of most particles is 40 μm < cfp < 500 μm, and preferably, when the density (pp) is 4 g / cm 3 When, the particle size of most particles is 60 μm < cfp < 500 μm, and when the density (pp) is 1 g / cm 3 When, the particle size of most particles is 250 μm < cfp < 100 μm.

[0039] The presently disclosed embodiments will now be described in detail in the context of Figure 4 the reactor system 103. However, it should be understood that the principles disclosed and taught herein can be applied to other systems that utilize different system components oriented in different ways, or different reaction schemes that utilize various catalyst compositions and chemical reactants. For example, the concepts described can be equivalently applied to other systems having alternative reactor units and regeneration units, such as those operating under non-fluidized conditions, or those including downcomers instead of risers. It should also be understood that not all parts of Figure 4 the reactor system are to be construed as being necessary to the claimed subject matter.

[0040] Now referring to Figure 4 , an example reactor system 103 that can be applicable to the methods and / or apparatuses described herein is schematically depicted. The reactor system 103 generally includes a plurality of system components, such as a reactor section 206 and a regeneration unit 306. As described herein, a "system component" refers to the various parts of the reactor system 103, such as reactors, separators, transfer lines, combinations thereof, and the like. As used herein in the context of Figure 4 the reactor section 206 generally refers to the part of the reactor system 103 where the primary process reaction (e.g., dehydrogenation) occurs to form the product stream. The reactor section 206 includes a reactor 202, which can include an upstream reactor section 254 and a downstream reactor section 230. Figure 4 The reactor 202 of Figure 4 can correspond to Figure 4As depicted, the reactor section 206 may additionally include a particulate solid separation section 214 for separating the catalyst from the chemical products formed in the reactor 202. Also as used herein, the regeneration unit 306 generally refers to the portion of the reactor system 103 that processes the particulate solids in some manner. As used herein, the regeneration unit 306 generally refers to the portion of the reactor system 103 that processes the particulate solids in some manner (such as by combustion) to, for example, improve the catalytic activity and / or heat the catalyst. The regeneration unit 306 may include a burner 355 and a riser 330, a particulate solid separation section 316, and may additionally include an oxygen treatment zone 370. In one or more embodiments, the particulate solid separation section 214 may be in fluid communication with the burner 355 (e.g., via a standpipe 426), and the particulate solid separation section 316 may be in fluid communication with the upstream reactor section 254 (e.g., via a standpipe 424 and a transport riser 430). In one or more embodiments, the chemical treatment vessel 400 may correspond to the burner 355. Although Figure 4 not shown in the figures, it is contemplated that a particulate solid distributor 100 may be utilized in the burner 355 to distribute the particulate solids.

[0041] Generally speaking, as described herein, in Figure 4 the depicted embodiments, a portion of the particulate solids is cycled between the reactor section 206 and the regeneration unit 306. It should be understood that when referring to particulate solids herein, they may refer to solid materials that are catalytically active for the desired reaction, or may equally refer to other particulate solids that are not necessarily catalytically active but affect the reaction, such as oxygen carrier materials, as referred to in the context of the Figure 4 system. The terms “catalytic activity” and “catalyst activity” refer to the extent to which a catalyst is able to catalyze the reactions occurring in the reactor system 103. The particulate solids exiting the reactor section 206 may be deactivated particulate solids. As used herein, “deactivated” may refer to a catalyst having a reduced catalytic activity or a colder catalyst compared to the catalyst entering the reactor section 206. However, the deactivated catalyst may retain some catalytic activity. The reduced catalytic activity may be caused by contamination with substances such as coke. Reactivation (sometimes referred to herein as “regeneration”) may remove contaminants such as coke, raise the temperature of the catalyst, or both. In an embodiment, the deactivated catalyst may be reactivated by catalyst reactivation in the regeneration unit 306. The deactivated catalyst may be reactivated by, but not limited to, removing coke by combustion, restoring the catalyst acidity, oxidizing the catalyst, other reactivation processes, or combinations thereof. In some embodiments, the catalyst may be heated during reactivation by burning fuels such as hydrogen, methane, ethane, propane, natural gas, or combinations thereof. The regenerated catalyst from the regeneration unit 306 may then be passed back to the reactor section 206.

[0042] As described with respect to Figure 4 the feed stream may enter the feed inlet 434, enter the reactor 202, and the product stream may exit the reactor system 103 via line 420. According to one or more embodiments, the reactor system 103 may be operated by feeding a chemical feed (e.g., in the feed stream) and a fluidized particulate solid into an upstream reactor section 254. The fluidized particulate solid may be fed into the upstream reactor section 254 via a particulate solid distributor 100. The chemical feed contacts the particulate solid in the upstream reactor section 254, and each chemical feed flows upwardly into and through the downstream reactor section 230 to produce a chemical product.

[0043] Referring now in detail to Figure 4 , the reactor section 206 may include an upstream reactor section 254, a transition section 258, and a downstream reactor section 230, such as a riser. The transition section 258 may connect the upstream reactor section 254 to the downstream reactor section 230. As Figure 4 depicted, the upstream reactor section 254 may be positioned below the downstream reactor section 230. Such a configuration may be referred to as an upflow configuration in the reactor 202. The upstream reactor section 254 may include a vessel, a drum, a barrel, or other vessel suitable for a given chemical reaction. As Figure 4 depicted, the upstream reactor section 254 may be connected to the downstream reactor section 230 via the transition section 258. The upstream reactor section 254 may generally include a larger cross-sectional area than the downstream reactor section 230. The transition section 258 may taper from the size of the cross-section of the upstream reactor section 254 to the size of the cross-section of the downstream reactor section 230 such that the transition section 258 projects inwardly from the upstream reactor section 254 into the downstream reactor section 230. For example, the transition section 258 may be a frustum.

[0044] The upstream reactor section 254 may be connected to a transport riser 430 which, in operation, may provide regenerated particulate solids in a feed stream to the reactor section 206. The particulate solids may enter the reactor 202 through a particulate solid distributor 100. The particulate solids entering the upstream reactor section 254 via the transport riser 430 may be transferred to the transport riser 430 through a standpipe 424 and thus arrive from the regeneration unit 306. A portion of the particulate solids may come directly from the particulate solid separation section 214 via a standpipe 422 and enter the transport riser 430, where this portion of the particulate solids enters the upstream reactor section 254. This particulate solids may be slightly deactivated, but in some embodiments may still be suitable for reaction in the upstream reactor section 254, particularly when used in combination with the regenerated particulate solids. The regenerated particulate solids arriving from the regeneration unit 306 and the portion of the deactivated particulate solids arriving from the particulate solid separation section 214 via the standpipe 422 may be kept separate within the transport riser 430 before being transferred to the reactor 202 via the particulate solid distributor 100, respectively.

[0045] Still referring Figure 4 , in one or more embodiments, based on the shape, size, and other processing conditions (such as temperature and pressure) in the upstream reactor section 254 and the downstream reactor section 230, the upstream reactor section 254 may operate as a fluidized bed, such as in a fast fluidized, turbulent, or bubbling bed upflow reactor, while the downstream reactor section 230 may operate in a more plug flow manner, such as in a riser reactor. For example, Figure 4 the reactor 202 may include an upstream reactor section 254 operating as a fast fluidized, turbulent, or bubbling bed reactor and a downstream reactor section 230 operating as a dilute phase riser reactor, such that the average particulate solids and gas flow move upward simultaneously. As used herein, the term "average flow" refers to the net flow, i.e., the total upward flow minus the reverse or backflow, which is typically characteristic of fluidized particles. As described herein, a "fast fluidized" reactor may refer to a reactor utilizing a fluidization scheme in which the superficial velocity of the gas phase is greater than the choking velocity and may be semi-dense in operation. As described herein, a "turbulent" reactor may refer to a fluidization scheme in which the superficial velocity is less than the choking velocity and is denser than the fast fluidization scheme. As described herein, a "bubbling bed" reactor may refer to a fluidization scheme in which distinct bubbles exist in a highly dense bed in two clearly defined phases. The "choking velocity" is the minimum velocity required to maintain solids in a dilute phase mode in a vertical transport line. As described herein, a "dilute phase riser" may refer to a riser reactor operating at a transport velocity where the gas and particulate solids have approximately the same velocity in the dilute phase.

[0046] According to an embodiment, the chemical product and the particulate solid can be transferred from the downstream reactor section 230 to the separation device 226 in the particulate solid separation section 214, where the particulate solid is separated from the chemical product, and the chemical product is conveyed out from the particulate solid separation section 214. According to one or more embodiments, after the particulate solid is separated from the vapor in the separation device 226, the particulate solid can generally move through the stripping zone 224 to the particulate solid outlet port 222, where the particulate solid is conveyed out of the reactor section 206 via the standpipe 426 and into the regeneration unit 306.

[0047] Still referring to Figure 4 , according to one or more embodiments, the separation device 226 can be a cyclone separation system, which can include two or more cyclone separation stages. In an embodiment where the separation device 226 includes more than one cyclone separation stage, the first separation device into which the fluidized stream enters is referred to as the primary cyclone separation device. The fluidized effluent from the primary cyclone separation device can enter the secondary cyclone separation device for further separation. The primary cyclone separation device can include, for example, a primary cyclone separator and systems commercially available under the names VSS (commercially available from UOP), LD2 (commercially available from Stone and Webster), and RS2 (commercially available from Stone and Webster). The primary cyclone separator is described, for example, in U.S. Patent Nos. 4,579,716, 5,190,650, and 5,275,641, each of which is incorporated herein by reference in its entirety. In some separation systems using a primary cyclone separator as the primary cyclone separation device, one or more additional sets of cyclone separators, for example, secondary cyclone separators and tertiary cyclone separators, are used to further separate the particulate solid from the product gas. It should be understood that any primary cyclone separation device can be used in the embodiments of the present invention.

[0048] Still referring to Figure 4 , the separated particulate solid is transferred from the particulate solid separation section 214 to the burner 355. In the burner 355, the particulate solid can be treated, for example, by combustion with oxygen. For example but not limited to, the particulate solid can be a decoked and / or combustible fuel to heat the particulate solid. In one or more embodiments, the particulate solid 100 can be passed through the particulate solid distributor 100 ( Figure 4(not shown in the figure) is transferred into the burner. Then, the granular solid is transferred out of the burner 355 and passed through the riser 330 to the riser termination separator 378, where the gas and solid components from the riser 330 are at least partially separated. The vapor and the remaining solid are transported to the secondary separation device 326 in the granular solid separation section 316, where the remaining granular solid is separated from the gas from the granular solid treatment (e.g., the gas emitted by burning the used granular solid or fuel, referred to as flue gas herein). The flue gas can be transferred out of the regeneration unit 306 via the outlet pipe 432. Then, the separated granular solid is passed through the standpipe 424 and the transport riser 430 to the oxygen treatment zone 370 within the granular solid separation section 316 to the upstream reactor section 254, where the granular solid is further used for the catalytic reaction. Thus, in operation, the granular solid can be circulated between the reactor section 206 and the regeneration unit 306. Generally speaking, the processed chemical stream including the feed stream and the product stream can be gaseous, and the granular solid can be a fluidized granular solid.

[0049] Now referring to the regeneration unit 306, as Figure 4 depicted, the burner 355 of the regeneration unit 306 can include one or more lower reactor section inlet ports 356 and can be in fluid communication with the riser 330. The oxygen-containing gas (such as air) can be transferred into the burner 355 through the pipe 428. The burner 355 can be in fluid communication with the granular solid separation section 214 via the standpipe 426, which can supply the used granular solid from the reactor section 206 to the regeneration unit 306 for regeneration. The burner 355 and the riser 330 (collectively referred to as the granular solid combustion reactor 302) can be operated with a fluidization scheme similar to or the same as the fluidization scheme disclosed for the upstream reactor section 254 and the downstream reactor section 230 of the reactor section 206. That is, the burner 355 can operate as a fluidized bed, such as in a fast fluidization, turbulent, or bubbling bed upflow reactor, while the riser 330 can be operated in a more plug flow manner, such as in a riser reactor. The geometries described with respect to the upstream reactor section 254 and the downstream reactor section 230 can equally apply to the burner 355 and the riser 330. Additionally, the burner 355 can further include a fuel inlet 354, which can supply a fuel such as a hydrocarbon feed stream or hydrogen to the burner 355. In one or more embodiments, the burner 355 can be Figure 3 a chemical treatment vessel 400.

[0050] As described in one or more embodiments, after separating particulate solids from the flue gas in the riser termination separator 378 and the secondary separation device 326, the treated particulate solids are treated with an oxygen-containing gas in the oxygen treatment zone 370. In some embodiments, the oxygen treatment zone 370 includes a fluid-solid contacting device. The fluid-solid contacting device may include a baffle or grid structure to promote contact between the treated particulate solids and the oxygen-containing gas. Examples of the fluid-solid contacting device are described in further detail in U.S. Patent Nos. 9,827,543 and 9,815,040. The fluidization regime within the oxygen treatment zone 370 may be of the bubbling bed type. The oxygen treatment zone 370 may include an oxygen-containing gas inlet 372 that supplies the oxygen-containing gas to the oxygen treatment zone 370 for oxygen treatment of the particulate solids.

[0051] Now returning to Figure 3 , in a non-limiting example, the chemical treatment vessel 400 described herein can be used to produce olefinic compounds from a hydrocarbon feed stream. As used herein, the term "olefinic compound" refers to a hydrocarbon having one or more carbon-carbon double bonds other than the formal double bonds in aromatic compounds. For example, ethylene and styrene are olefinic compounds, but ethylbenzene is not an olefinic compound because the only double bond present in ethylbenzene is a formal double bond that is part of an aromatic structure. Olefinic compounds can be produced from various hydrocarbon feed streams by utilizing different reaction mechanisms. For example, olefinic compounds can be produced by at least dehydrogenation reactions, cracking reactions, dehydration reactions, and methanol-to-olefins reactions. These reaction types can utilize different feed streams and different fluidized particles to produce olefinic compounds. Considering Figure 3 the particulate solid distributor 100 and the chemical treatment vessel 400 can be used to carry out reactions in reactor systems other than those described in the context of the Figure 4 reactor system 103.

[0052] According to one or more embodiments, the reaction can be a dehydrogenation reaction. According to such embodiments, one or more hydrocarbons can be a hydrocarbon feed stream, which can include one or more of ethylbenzene, ethane, propane, n-butane, and isobutane. In one or more embodiments, the hydrocarbon feed stream can contain at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% of ethylbenzene. In one or more embodiments, the hydrocarbon feed stream can contain at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% of ethane. In additional embodiments, the hydrocarbon feed stream can contain at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% of propane. In additional embodiments, the hydrocarbon feed stream can contain at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% of n-butane. In additional embodiments, the hydrocarbon feed stream can contain at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% of isobutane. In additional embodiments, the hydrocarbon feed stream can contain at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% of the sum of ethylbenzene, ethane, propane, n-butane, and isobutane.

[0053] In one or more embodiments, the dehydrogenation reaction can utilize gallium and / or platinum fluidized particles as a catalyst. In such embodiments, the fluidized particles can include a gallium and / or platinum catalyst. As described herein, the gallium and / or platinum catalyst contains gallium, platinum, or both. The gallium and / or platinum catalyst can be supported by an alumina or alumina-silica support and can optionally contain potassium. Such gallium and / or platinum catalysts are disclosed in U.S. Patent No. 8,669,406, which is incorporated herein by reference in its entirety. However, it should be understood that other suitable catalysts can be utilized for the dehydrogenation reaction.

[0054] In one or more embodiments, the reaction mechanism can be dehydrogenation followed by combustion (in the same chamber). In such embodiments, the dehydrogenation reaction can produce hydrogen as a byproduct, and the oxygen carrier material can contact the hydrogen and promote its combustion to form water. Examples of such reaction mechanisms are disclosed in WO 2020 / 046978 and U.S. Patent Publication No. 2021 / 0292259, which are considered to be possible reaction mechanisms for the systems and methods described herein, and the teachings of these documents are incorporated herein by reference in their entirety.

[0055] In one or more embodiments, the fluidized particles can comprise an oxygen carrier material and a dehydrogenation catalyst material. In some embodiments, the fluidized particles can consist essentially of the oxygen carrier material. As used herein, "consisting essentially of" means a material having less than 1 wt% of unenumerated materials (i.e., consisting essentially of A means that A comprises at least 99 wt% of the composition). In some embodiments, the fluidized particles can not comprise a dehydrogenation catalyst material. In some embodiments, the oxygen carrier material and the dehydrogenation catalyst material can be separate particles of the fluidized particles. In some embodiments, the oxygen carrier material and the dehydrogenation catalyst can be contained within the same particle of the fluidized particles.

[0056] In embodiments where the fluidized particles comprise a dehydrogenation catalyst, the dehydrogenation of one or more hydrocarbons can occur at least in part via catalytic dehydrogenation. Catalytic dehydrogenation is the dehydrogenation of a hydrocarbon facilitated by the use of a dehydrogenation catalyst. In embodiments where the fluidized particles do not comprise a dehydrogenation catalyst, the dehydrogenation reaction can be a non-catalytic thermal dehydrogenation reaction. Non-catalytic thermal dehydrogenation refers to the dehydrogenation of a hydrocarbon that occurs due to high temperature without the use of a dehydrogenation catalyst.

[0057] In some embodiments, the fluidized particles can comprise a "dual-use material" that can act as both a dehydrogenation catalyst and an oxygen carrier material. It should be understood that in at least those embodiments where the oxygen carrier material and the dehydrogenation catalyst described herein are used in the same reaction vessel (such as Figure 1 the reaction vessel), such a dual-use material can be used in place of or in combination with the oxygen carrier material and the dehydrogenation catalyst of the fluidized particles.

[0058] According to one or more embodiments, the reaction can be a cracking reaction. According to such embodiments, the hydrocarbon feed stream can comprise one or more of naphtha, n-butane, or isobutane. According to one or more embodiments, the hydrocarbon feed stream can comprise at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% of naphtha. In additional embodiments, the hydrocarbon feed stream can comprise at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% of n-butane. In additional embodiments, the hydrocarbon feed stream can comprise at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% of isobutane. In additional embodiments, the hydrocarbon feed stream can comprise at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% of the combined total of naphtha, n-butane, and isobutane.

[0059] In one or more embodiments, the cracking reaction can utilize one or more zeolites as a catalyst. In such embodiments, the fluidized particles can comprise one or more zeolites. In some embodiments, the one or more zeolites utilized in the cracking reaction can comprise ZSM-5 zeolite. However, it should be understood that other suitable catalysts can be utilized for the cracking reaction. For example, suitable commercially available catalysts can include Intercat Super Z Excel or Intercat Super Z Exceed. In additional embodiments, in addition to the catalytically active material, the cracking catalyst can further comprise platinum. For example, the cracking catalyst can comprise from 0.001 wt% to 0.05 wt% of platinum. The platinum can be sprayed on as platinum nitrate and calcined at an elevated temperature (such as about 200 °C to 800 °C). Without being bound by theory, it is believed that adding platinum to the catalyst can allow for easier combustion of fuels such as methane.

[0060] According to one or more embodiments, the reaction can be a dehydration reaction. According to such embodiments, the hydrocarbon feed stream can contain one or more of ethanol, propanol, or butanol. According to one or more embodiments, the hydrocarbon feed stream can contain at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% ethanol. In additional embodiments, the hydrocarbon feed stream can contain at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% propanol. In additional embodiments, the hydrocarbon feed stream can contain at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% butanol. In additional embodiments, the hydrocarbon feed stream can contain at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% of the total of ethanol, propanol, and butanol.

[0061] In one or more embodiments, the dehydration reaction can utilize one or more acid catalysts. In such embodiments, the fluidized particles can include one or more acid catalysts. In some embodiments, the one or more acid catalysts utilized in the dehydration reaction can include zeolites (such as ZSM-5 zeolite), alumina, amorphous aluminosilicate, acidic clay, or combinations thereof. For example, according to one or more embodiments, commercially available alumina catalysts that may be suitable include SynDol (available from Scientific Design Company), V200 (available from UOP), or P200 (available from Sasol). Commercially available zeolite catalysts that may be suitable include CBV 8014, CBV 28014 (each available from Zeolyst). Commercially available amorphous aluminosilicate catalysts that may be suitable include silica-alumina catalyst support, grade 135 (available from Sigma Aldrich). However, it should be understood that other suitable catalysts can be utilized for the dehydration reaction.

[0062] According to one or more embodiments, the reaction can be a methanol-to-olefins reaction. According to such embodiments, the hydrocarbon feed stream can contain methanol. According to one or more embodiments, the hydrocarbon feed stream can contain at least 50 wt%, at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, or even at least 99 wt% methanol.

[0063] In one or more embodiments, the methanol - to - olefins reaction can utilize one or more zeolites as catalysts. In such embodiments, the fluidized particles can include one or more zeolites. In some embodiments, the one or more zeolites utilized in the methanol - to - olefins reaction can include one or more of ZSM - 5 zeolite or SAPO - 34 zeolite. However, it should be understood that other suitable catalysts can be utilized to carry out the methanol - to - olefins reaction.

[0064] In one or more embodiments, olefinic compounds can be present in a "product stream" sometimes referred to as an "olefin - containing effluent". This stream leaves Figure 4 the reactor system and can subsequently be processed. In one or more embodiments, the olefinic compounds can include one or more of ethylene, propylene, butene, or styrene. The term butene includes any butene isomer, such as α - butene, cis - β - butene, trans - β - butene, and isobutene. In some embodiments, the olefin - containing effluent can contain at least 20 wt%, at least 30 wt%, at least 40 wt%, at least 50 wt%, or even at least 60 wt% of ethylene. In additional embodiments, the olefin - containing effluent can contain at least 20 wt%, at least 30 wt%, at least 40 wt%, at least 50 wt%, or even at least 60 wt% of propylene. In additional embodiments, the olefin - containing effluent can contain at least 20 wt%, at least 30 wt%, at least 40 wt%, at least 50 wt%, or even at least 60 wt% of butene. In additional embodiments, the olefin - containing effluent can contain at least 20 wt%, at least 30 wt%, at least 40 wt%, at least 50 wt%, or even at least 60 wt% of styrene. In additional embodiments, the olefin - containing effluent can contain at least 20 wt%, at least 30 wt%, at least 40 wt%, at least 50 wt%, or even at least 60 wt% of the sum of ethylene, propylene, butene, and styrene. The olefin - containing effluent can also contain unreacted components of the feed stream and other reaction products that are not considered light olefins. The olefinic compounds can be separated from the unreacted components in subsequent separation steps.

[0065] In a first aspect of the present disclosure, a granular solid dispenser adapted to dispense two granular solid streams may include an inner conduit that extends from an inner conduit inlet to an inner conduit outlet. The inner conduit may be at least partially defined by an inner wall, and the inner wall may be arranged around a central axis. The granular solid dispenser may further include an outer conduit that is at least partially defined by the inner wall and an outer wall. The outer conduit may extend from an outer conduit inlet to an outer conduit outlet. The outer wall may be arranged around the central axis, and a cross-section of the outer wall may enclose a cross-section of the inner wall in a plane perpendicular to the central axis. The granular solid dispenser may further include a first solid guide positioned above the central axis and downstream of the inner conduit outlet. The granular solid dispenser may further include a second solid guide attached to the inner wall and extending radially outward from the central axis. The inner conduit may extend through the outer conduit such that the inner conduit outlet may be located downstream of the outer conduit outlet.

[0066] A second aspect of the present disclosure includes any previous aspect or combination of aspects, wherein the first solid guide is a first deflector plate and the second solid guide is a second deflector plate.

[0067] A third aspect of the present disclosure includes any previous aspect or combination of aspects, wherein the inner wall has a cross-sectional shape that is circular, oval, elliptical, or polygonal in a plane perpendicular to the central axis, and the outer wall has a cross-sectional shape that is circular, oval, elliptical, or polygonal in a plane perpendicular to the central axis.

[0068] A fourth aspect of the present disclosure includes any previous aspect or combination of aspects, wherein the inner wall has a circular cross-sectional shape in a plane perpendicular to the central axis, and the outer wall has a circular cross-sectional shape in a plane perpendicular to the central axis.

[0069] A fifth aspect of the present disclosure includes any previous aspect or combination of aspects, wherein the inner conduit outlet is located downstream of the second solid guide.

[0070] In a sixth aspect of the present disclosure, a granular solid dispenser adapted to dispense two streams of granular solids may include an inner conduit extending from an inner conduit inlet to an inner conduit outlet. The inner conduit may be at least partially defined by an inner wall, and the inner wall may be arranged around a central axis. The granular solid dispenser may further include an outer conduit at least partially defined by the inner wall and an outer wall. The outer conduit may extend from an outer conduit inlet to an outer conduit outlet. The outer wall may be arranged around the central axis. A cross-section of the outer wall may enclose a cross-section of the inner wall in a plane perpendicular to the central axis. The granular solid dispenser may further include an inlet conduit at least partially defined by an inlet conduit wall. The inlet conduit may extend from an inlet conduit inlet to an inlet conduit outlet. The inlet conduit may intersect the outer wall. The inlet conduit outlet may be positioned at the inner wall such that the inlet conduit may communicate with the inner conduit. The granular solid dispenser may further include a first solid guide positioned above the central axis and downstream of the inner conduit outlet. The granular solid dispenser may further include a second solid guide attached to the inner wall and extending radially outward from the central axis. The inner conduit may extend through the outer conduit such that the inner conduit outlet may be located downstream of the outer conduit outlet.

[0071] A seventh aspect of the present disclosure includes the sixth aspect, wherein the first solid guide is a first deflector plate and the second solid guide is a second deflector plate.

[0072] An eighth aspect of the present disclosure, alone or in any combination, includes the sixth aspect or the seventh aspect, wherein the inner wall has a cross-sectional shape that is circular, oval, elliptical, or polygonal in a plane perpendicular to the central axis, and the outer wall has a cross-sectional shape that is circular, oval, elliptical, or polygonal in a plane perpendicular to the central axis.

[0073] A ninth aspect of the present disclosure, alone or in any combination, includes the sixth aspect to the eighth aspect, wherein the inner wall has a circular cross-sectional shape in a plane perpendicular to the central axis, and the outer wall has a circular cross-sectional shape in a plane perpendicular to the central axis.

[0074] A tenth aspect of the present disclosure, alone or in any combination, includes the sixth aspect to the ninth aspect, wherein the inner conduit outlet is located downstream of the second solid guide.

[0075] In an eleventh aspect of the present disclosure, a granular solid dispenser for dispensing two granular solid streams may include an inner conduit extending from an inner conduit inlet to an inner conduit outlet. The inner conduit may be at least partially defined by an inner wall. The inner wall may be arranged around a central axis. The granular solid dispenser may further include an outer conduit at least partially defined by the inner wall and an outer wall. The outer conduit may extend from an outer conduit inlet to an outer conduit outlet. The outer wall may be arranged around the central axis. A cross-section of the outer wall may enclose a cross-section of the inner wall in a plane perpendicular to the central axis. The granular solid dispenser may further include an inlet conduit at least partially defined by an inlet conduit wall. The inlet conduit may extend from an inlet conduit inlet to an inlet conduit outlet. The inlet conduit outlet may be positioned at the outer wall such that the inlet conduit may communicate with the outer conduit. The granular solid dispenser may further include a first solid guide positioned above the central axis and downstream of the inner conduit outlet. The granular solid guide may further include a second solid guide attached to the inner wall and extending radially outward from the central axis. The inner conduit may extend through the outer conduit such that the inner conduit outlet may be located downstream of the outer conduit outlet.

[0076] A twelfth aspect of the present disclosure includes the eleventh aspect, wherein the first solid guide is a first deflector plate and the second solid guide is a second deflector plate.

[0077] A thirteenth aspect of the present disclosure, alone or in any combination, includes the eleventh aspect or the twelfth aspect, wherein the inner wall has a cross-sectional shape that is circular, oval, elliptical, or polygonal in a plane perpendicular to the central axis, and the outer wall has a cross-sectional shape that is circular, oval, elliptical, or polygonal in a plane perpendicular to the central axis.

[0078] A fourteenth aspect of the present disclosure, alone or in any combination, includes the eleventh to thirteenth aspects, wherein the inner wall has a circular cross-sectional shape in a plane perpendicular to the central axis, and the outer wall has a circular cross-sectional shape in a plane perpendicular to the central axis.

[0079] A fifteenth aspect of the present disclosure, alone or in any combination, includes the eleventh to fourteenth aspects, wherein the inner conduit outlet is located downstream of the second solid guide.

[0080] It will be apparent to those skilled in the art that various modifications and variations can be made to the technology disclosed in this invention without departing from the spirit and scope of the technology. Since those skilled in the art can make modifications, combinations, sub - combinations, and variations of the disclosed embodiments that incorporate the spirit and substance of the technology disclosed in this invention, this technology should be construed to include all things within the scope of the appended claims and their equivalents. Additionally, although some aspects of this disclosure may be identified herein as preferred or particularly advantageous, it is contemplated that this disclosure is not limited to these aspects.

[0081] It should be noted that the various details described in this disclosure should not be taken to imply that these details relate to elements that are fundamental components of each of the embodiments described in this disclosure, even in cases where a particular element is shown in each of the drawings appended to this specification. Unless explicitly stated otherwise, none of the features disclosed and described herein should be construed as "essential". The contemplated embodiments of this technology include those that incorporate some or all of the features of the appended claims.

[0082] It should be understood that in some embodiments, the compositional ranges of chemical components in a stream or reactor should be understood to contain mixtures of isomers of that component. For example, a specified compositional range of butene can include mixtures of the various isomers of butene. It should be understood that the examples provide compositional ranges for various streams, and the total amounts of isomers of a particular chemical composition can constitute a range.

[0083] It should be noted that one or more of the following claims and detailed description utilize the terms "where" or "wherein" as transitional phrases. For the purpose of defining this technology, it should be noted that this term is introduced in the claims as an open - ended transitional phrase that is used to introduce a recitation of a series of characteristics of a structure, and should be interpreted in a manner similar to the more commonly used open - ended preamble term "comprising".

[0084] It should be understood that any two quantitative values assigned to a characteristic can constitute a range of that characteristic, and all combinations of ranges formed by all of the recited quantitative values of a given characteristic are contemplated in this disclosure. In cases where multiple ranges of quantitative values are provided, these ranges can be combined to form a broader range, which is contemplated in the embodiments described herein.

[0085] As understood in the context of the terms used herein, the term "transfer" can include directly transferring a substance between two parts of the disclosed system, and in some cases, means indirectly transferring a substance between two parts of the disclosed system. For example, indirect transfer can include steps in which the substance transfer occurs through intermediate operating units, valves, sensors, etc.

Claims

1. A granular solid dispenser adapted to dispense two flows of granular solids, the granular solid dispenser comprising: an inner conduit extending from an inner conduit inlet to an inner conduit outlet, wherein the inner conduit is at least partially defined by an inner wall, and wherein the inner wall is arranged around a central axis 600; an outer conduit at least partially defined by the inner wall and an outer wall, wherein the outer conduit extends from an outer conduit inlet to an outer conduit outlet, wherein the outer wall is arranged around the central axis 600, and wherein a cross-section of the outer wall encloses a cross-section of the inner wall in a plane perpendicular to the central axis 600; a first solid guide positioned above the central axis 600 and downstream of the inner conduit outlet; and a second solid guide attached to the inner wall and extending radially outward from the central axis 600; and wherein: the inner conduit extends through the outer conduit such that the inner conduit outlet is downstream of the outer conduit outlet.

2. The granular solid dispenser according to claim 1, wherein the first solid guide is a first deflector plate and the second solid guide is a second deflector plate.

3. The granular solid dispenser according to any one of the preceding claims, wherein the inner wall has a cross-sectional shape that is circular, oval, elliptical or polygonal in a plane perpendicular to the central axis, and the outer wall has a cross-sectional shape that is circular, oval, elliptical or polygonal in a plane perpendicular to the central axis.

4. The granular solid dispenser according to any one of the preceding claims, wherein the inner wall has a circular cross-sectional shape in a plane perpendicular to the central axis, and the outer wall has a circular cross-sectional shape in a plane perpendicular to the central axis.

5. The granular solid dispenser according to any one of the preceding claims, wherein the inner conduit outlet is downstream of the second solid guide.

6. A granular solid dispenser adapted to dispense two flows of granular solids, the granular solid dispenser comprising: an inner conduit extending from an inner conduit inlet to an inner conduit outlet, wherein the inner conduit is at least partially defined by an inner wall, and wherein the inner wall is arranged around a central axis; an outer conduit at least partially defined by the inner wall and an outer wall, wherein the outer conduit extends from an outer conduit inlet to an outer conduit outlet, wherein the outer wall is arranged around the central axis, and wherein a cross-section of the outer wall encloses a cross-section of the inner wall in a plane perpendicular to the central axis; an inlet conduit at least partially defined by an inlet conduit wall, wherein the inlet conduit extends from an inlet conduit inlet to an inlet conduit outlet, wherein the inlet conduit intersects the outer wall, and wherein the inlet conduit outlet is positioned at the inner wall such that the inlet conduit is in communication with the inner conduit; a first solid guide positioned above the central axis and downstream of the inner conduit outlet; and a second solid guide attached to the inner wall and extending radially outwardly from the central axis; and wherein the inner conduit extends through the outer conduit such that the inner conduit outlet is downstream of the outer conduit outlet.

7. The particulate solid dispenser according to claim 6, wherein the first solid guide is a first deflector plate and the second solid guide is a second deflector plate.

8. The particulate solid dispenser according to claim 6 or 7, wherein the inner wall has a cross-sectional shape that is circular, oval, elliptical or polygonal in a plane perpendicular to the central axis, and the outer wall has a cross-sectional shape that is circular, oval, elliptical or polygonal in a plane perpendicular to the central axis.

9. The particulate solid dispenser according to claims 6 to 8, wherein the inner wall has a circular cross-sectional shape in a plane perpendicular to the central axis, and the outer wall has a circular cross-sectional shape in a plane perpendicular to the central axis.

10. The particulate solid dispenser according to claims 6 to 9, wherein the inner conduit outlet is downstream of the second solid guide.

11. A particulate solid dispenser adapted to dispense two particulate solid streams, the particulate solid dispenser comprising: an inner conduit extending from an inner conduit inlet to an inner conduit outlet, wherein the inner conduit is at least partially defined by an inner wall, and wherein the inner wall is arranged around a central axis; an outer conduit at least partially defined by the inner wall and an outer wall, wherein the outer conduit extends from an outer conduit inlet to an outer conduit outlet, wherein the outer wall is arranged around the central axis, and wherein the cross-section of the outer wall encloses the cross-section of the inner wall in a plane perpendicular to the central axis; an inlet conduit at least partially defined by an inlet conduit wall, wherein the inlet conduit extends from an inlet conduit inlet to an inlet conduit outlet, and wherein the inlet conduit outlet is positioned at the outer wall such that the inlet conduit is in communication with the outer conduit; a first solid guide positioned above the central axis and downstream of the inner conduit outlet; and a second solid guide attached to the inner wall and extending radially outwardly from the central axis; and wherein the inner conduit extends through the outer conduit such that the inner conduit outlet is downstream of the outer conduit outlet.

12. The particulate solid dispenser according to claim 11, wherein the first solid guide is a first deflector plate and the second solid guide is a second deflector plate.

13. The particulate solid dispenser according to claim 11 or 12, wherein the inner wall has a cross-sectional shape that is circular, oval, elliptical or polygonal in a plane perpendicular to the central axis, and the outer wall has a cross-sectional shape that is circular, oval, elliptical or polygonal in a plane perpendicular to the central axis.

14. The granular solid dispenser according to claims 11 to 13, wherein the inner wall has a circular cross-sectional shape in a plane perpendicular to the central axis, and the outer wall has a circular cross-sectional shape in a plane perpendicular to the central axis.

15. The granular solid dispenser according to claims 11 to 14, wherein the inner conduit outlet is located downstream of the second solid guide.

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