SA519410056B1 - Systems and methods for uprating dehydrogenation reactors - Google Patents

Abstract

A catalytic reactor is disclosed. The catalytic reactor includes one or more nonporous covers configured to cover a portion of each of the plurality of catalyst beds so that when the gas feed flows through the feed inlet into the catalytic reactor, the gas feed does not enter the plurality of catalyst beds at a section of each of the catalyst beds closest to the feed inlet. Instead, the gas feed enters each catalyst bed at another section of each of the catalyst beds.

Description

SYSTEMS AND METHODS FOR UPRATING DEHYDROGENATION

REACTORS

Full Description BACKGROUND The present invention generally relates to equipment used to perform chemical reactions in industrial processes. More specifically, the present invention relates to the bed reactor 860 being used. In dehydrogenating hydrocarbons 5 Jie Olefins propylene and oly wld ethylene petroleum are important for many polymers and intermediates 6 11 101607601. Olefins are characterized by their double bond, and one of the methods of producing olefins is the dehydrogenation of other hydrocrions (Jie paraffins) to form a double bond and thus the formation of olefins. 0 Typically, the dehydrogenation reaction takes place in the presence of a catalyst, the dehydrogenation reactor, for example (Jal). <isobutane 1-butene ¢«1-butene and isopentane .isopentane as dale Catalytic dehydrogenation reactors are single bed flow down reactors. For example » US Patent No. 2,915,375 discloses a design for a single-layer dehydrogenation reactor (Gla) used in this industry. A fixed-bed reactor sometimes includes an inlet Jae distributor containing an array of circular or oval plates with a large central opening and one multi-hole plate at the bottom of the inlet distributor.0 Increases demand for olefins.However, operating olefin reactors in existing plants at feed rates higher than the design feed rates of the plants may lead to misdistribution and related problems by operating. Furthermore it; There is a potential solution to meet the growing demand

Expansion of the olefin industrial unit by installing parallel reactors. But this solution would require significant capital expenditures. General description of the invention A catalytic reactor with a fixed bed was discovered that flows the feedstock through the catalyst in the reactor in a way that increases the contact between the feedstock and the catalyst in the limited reactor space. The disclosed fixed bed catalytic reactor; according to the embodiments of the invention; By dividing the feedstock flow, the feedstock is directed to flow through the catalyst beds at an angle with the initial feedstock flow into the reactor to create an improved flow distribution. Embodiments of the invention include a catalytic reactor comprising one or more walls and a feed inlet configured to direct the flow of a 0 feed gas stream into the catalytic reactor. The catalytic reactor may also include a group of in-wall catalyst layers or GSTs where each catalyst layer includes a first end placed near the feed inlet; A second end is placed farther from the feeding entrance than the first end, the middle of a thread between the first end and the second end. The catalytic reactor may also include one or more nonporous covers placed between the feed inlet and the catalyst bed assembly and arranged to cover 5 part comprising the first end of each catalyst bed so as to largely or completely block the feed gas Entering the catalytic reactor from entering each catalyst bed at the first hall. Embodiments of the invention include a catalytic reactor comprising one or more walls wherein a cylindrical foley is formed. The catalytic reactor may include two catalyst layers placed within the cylindrical vessel and a feed inlet configured to direct the flow of a 0” feed gas stream into the catalytic reactor. The catalytic reactor may also include a non-porous Be prepared to cover oj from each of the two catalyst layers so that when the gas feed stream flows through the feed inlet to the catalytic reactor; The gas feed stream does not enter the two catalyst beds at a section in each of the two catalyst beds closest to the feed inlet nor does it enter the two catalyst beds in a direction parallel to the direction of flow of the gas feed stream through the feed inlet. INMAMA The gas feed stream enters each catalyst bed at another section for every 5 catalyst layers in a lateral and/or oblique direction to the direction of the gas feed stream flow through the feed inlet. The catalytic reactor may also include a central chamber between the two catalyst layers prepared to receive the gas

effluent from the catalyst layers. Furthermore it; The catalytic reactor may include a manifold under the catalyst bed. They keep the manifold in fluid communication with the central chamber. The manifold is also in contact by means of the fluid with one or more outlets which are intended for the flow of one or more gases from the manifold.

Embodiments of the invention include a method for dehydrogenation of hydrocrion. The method involves flowing a feed gas into a catalytic reactor through a feed inlet conditioned to direct a feed gas flow into the catalytic reactor. The catalytic reactor may have one or more walls and a set of catalyst layers placed within the wall or ST where each catalyst layer includes a first end placed near the dal inlet and an OB end placed further from the feed inlet than the first end” shag Middle subject between the first party

0 and the second party. The method may also include directing the incoming gas feed stream to the catalytic reactor so that it is largely or completely prevented from entering each catalyst bed at the first end; Routing is done using one or more non-porous sheaths placed between the feed inlet and the catalyst bed assembly. Embodiments of the invention include a method for retrofitting a catalytic reactor. The method involves providing a catalytic reactor

5 has a wall or SH where the Lge feed inlet is to direct the flow of a gas feed stream to the catalytic reactor; A group of catalyst layers is placed within one or more walls; Where each catalyst bed includes a first tip positioned near the feed inlet; A second party placed farther from the feeding entrance than the first party; And a middle part subject between the first party and the second party. The method may also include the addition of one or more non-porous sheaths between the feed inlet and the catalyst bed assembly so that:

0 One or more non-porous sheaths shall cover a portion comprising the first end of each bed of the group of catalyst layers and shall largely or completely prevent such feedstream gas entering the catalytic reactor from entering each catalyst bed at the first end. The following terms include definitions of the various terms and phrases used throughout the current specification.

5 The terms “around” or “nearly” are defined as close to as understood by a person of ordinary skill in the art. In one of the unrestricted embodiments; The two terms are defined as:

within 10 of thanks; Within 5 of, JST is preferred within 1 of, and most preferably within

20.5

The terms “7 by weight,” “7 by volume,” or “7 sala,” respectively; to weight or volume or

molar percentage of the component; Based on total weight, total volume, or total moles

The material that includes the component. In an example other than ce 10 moles of the ingredient are in 100 moles of the substance

It means 710 in the mole.

The term “pretty much” and its variations are defined on the ranges 710, 75, or 71

or 70.5.

include the terms anil, 'reduce', 'and' or 'avoid' or any variation thereof; 0 when used in claims and/or specifications; No measurable reduction or complete inhibition

to achieve the desired result.

the term 'active'; As this term is used in the specification and/or claims; it means that

Suitable for achieving a desired, expected or intended result.

the use of indefinite articles in combination with the term 'includes', 'including', 'contains' or 5 'therefore' in the claim or specification may mean 'one' but also correspond to the meaning of 'one or more';

'at least one' and 'one or more than one'.

the words 'include' (and any form of include; die 'include' and 'include');

on" (and in any form where contains; ie 'containing' and 'has'); 'including' (ie

form including; Jie 'include' and 'include' or 'contain' (and any form of 'contain'; such as 'contain' and 'contain' (le) are inclusive or open terms and do not exclude items or

Additional method steps or not mentioned.

The process of the present invention may include 'consisting of', 'consisting mainly of', or 'consisting of' components

certain combinations; etc.; disclosed throughout the specification.

In the context of the present invention; At least the following twenty incarnations are provided. Embodiment 1 relates to a 5 catalytic reactor. The catalytic reactor includes one or more walls; A feed inlet conditioned to direct the flow of a gas feed stream to the

catalytic reactor a group of catalyst layers placed within one or more walls; Where all include

first tip catalyst layer placed near the feed inlet; And a second party placed further from the feeding entrance than the first party; And a middle part placed between the first party and the second party; one or more

of non-porous film placed between the feed inlet and the catalyst bed assembly and prepared to cover

eda includes the first end of each catalyst layer group so that gas is largely prevented

5 Feed stream entering the catalytic reactor from entering each catalyst bed at the first end. Embodiment 2 relates to the catalytic reactor of Embodiment 1; In which two or more layers of catalyst are placed inside the wall. Embodiment 3 relates to the catalytic reactor of Embodiment 2 where the catalytic reactor has a shell

One non-porous surface fitted to cover the gia of each of the two catalyst layers. Embodiment 4 relates to the catalytic reactor of either Embodiments 2 or 3; The gas feed stream does not enter the two catalyst layers in one direction

10 parallel to the direction of flow of the gas feed stream through the feed inlet; day daly The gas feed stream to each catalyst bed is lateral and/or oblique to the direction of the gas feed stream flow through the feed inlet. Embodiment 5 relates to the catalytic reactor of any of Embodiments 1 to 4; The catalytic reactor includes a cylindrical vessel. Embodiment 6 relates to the catalytic reactor of any of Embodiments 2 to

5. It also includes a central chamber between the two shee catalyst layers to receive the gas flowing from

5 layers catalyst. Embodiment 7 relates to the catalytic reactor of embodiment 6 as it further comprises a manifold under the catalyst layers and in fluid contact with the central chamber. Embodiment 8 relates to the catalytic reactor of Embodiment 7 as it also includes one or more outlets in connection with

The fluid path with the manifold is provided for the flow of one or more gases from the manifold. Embodiment 9 relates to the catalytic reactor of Embodiment 8 where one or more of the gases comprises air at

0 Run a decarbonization cycle. Embodiment 10 relates to the catalytic reactor of embodiment 8; Where one or more of the gases contains a hydrocrion when the dehydrogenation cycle is running. Personification 11

relates to the catalytic reactor of any of Embodiments 1 to 10; Where one or more of the non-porous casings includes a roof shroud thermal arch refractory arch

12 relates to the catalytic reactor of any of embodiments 1 1 to 10; Where one or more

5. of non-porous casing on a SAE 310 LS stainless steel curved sheet metal. Embodiment 13 relates to the Gall reactor of any of Embodiments 1 1 to

Gua (10) One or more non-porous casings comprise a curved SAE 304 L stainless steel plate with polymeric coating/painting. Embodiment 14 relates to the catalytic reactor of any Of Embodiments 1 1 through 13, where dag one or more non-porous casings the gas feed flows alongside the walls before the inbound gas feed into the catalyst beds.

Embodiment 15 relates to a method for dehydrogenation of a hydrocarbon” wherein the method includes the step of flowing a feed gas into a catalytic reactor through a feed inlet prepared to direct a feed gas flow into the catalytic reactor; Where the catalytic reactor contains one or more walls and a set of catalyst layers placed inside the wall or iE where each catalyst layer includes a first end threaded from the inlet 0 feed; And a second party placed further from the feeding entrance than the first party; and ein is a middle subject between the first and the second party; directing the incoming gas feed stream to the catalytic reactor so that it is largely prevented from entering each catalyst bed at the first end; Routing is performed using one or more non-porous sheaths placed between the feed inlet and the catalyst bed assembly. embodiment 16 relates to the method for embodiment 15; It further includes a gas feed stream step such that the gas feed stream enters the catalyst bed assembly in a direction parallel to the gas feed stream flow direction through the feed inlet; Inmaa the gas feed stream enters each catalyst bed in a lateral and/or oblique direction to the flow direction of the gas feed stream through the feed inlet. Embodiment 17 relates to the method for embodiment Cua 6 also includes a gas product flow step from the catalyst beds into a central chamber between the final bedset) wherein the central chamber is prepared to receive the gas product flow from the catalyst beds. 0 Objective 18 relates to the method for Objective 17; It also includes the flow of gas product through a manifold

Under the catalyst layer and in contact via the fluid with the central chamber. Embodiment 19 relates to a method for reprocessing a catalytic reactor. The method for embodiment 19 includes a catalytic Jolin step involving one or more walls; Lge feed inlet to direct the flow of a gas feed stream to the catalytic reactor; A group of catalyst layers placed inside the wall or “JST” where each catalyst layer includes 5 first terminals placed near the feed inlet; A second end placed further from the feeding entrance than the first end, and a middle part placed between the first end and the second end; Add one or more covers

Non-porous between the feed inlet and the catalyst bed assemblies so that one or more non-porous sheaths cover a portion including the first end of each catalyst bed assemblage and this feed stream into the catalytic reactor is largely prevented from entering each catalyst bed at the first end. Embodiment 20 relates to the method for embodiment 19; Where one or more non-porous casings and one or more walls are prepared for the gas feed stream to enter each catalyst bed in a lateral and/or oblique direction to the gas feed stream flow direction through the feed inlet. The objectives, characteristics and other advantages of the present invention will be evident from the following figures, detailed description and examples. However, it must be understood that figures, detailed descriptions and examples are presented; with reference to specific embodiments of the invention; For illustration only and is not intended to be restrictive. additionally 0; Changes and modifications within the scope and content of the invention are expected to become apparent to those skilled in the art from this detailed description. in additional embodiments; Features of specific avatars can be combined with features of other avatars. For example Ji the properties of one embodiment may be combined with the properties of other embodiments. in additional embodiments; Additional properties can be added to the specific properties described here. 5 Brief Explanation of Drawings For a more complete understanding The following descriptions are now referenced in conjunction with accompanying drawings; in which: Figs. 11 and 1[b show frontal views of a fixed bed reactor for dehydrogenation of hydrocrions; according to the embodiments of the invention; 0 Fig. 2 shows a side view of the fixed bed reactor for clin So ua dehydrogenation according to embodiments of the invention; Figure 3 shows a method for dehydrogenation of hydrocarbons in a fixed bed reactor; according to the embodiments of the invention; and Fig. 4 shows a method for reprocessing the Jolie fixed bed for dehydrogenation of hydrocarbons; According to 5 embodiments of the invention. Detailed description:

A fixed bed catalytic reactor has been revealed that teaches the flow of feedstock through a catalyst in the reactor in such a way as to increase the contact between the feedstock and the catalyst in the limited space of the reactor. The fixed bed catalytic reactor of CRASH; According to the embodiments of the invention; Divide the feedstock flow and direct the feedstock to flow through the catalyst layers in the reactor at an angle with the initial feedstock flow in the reactor to create an improved flow distribution. The flow cross-sectional area of the incoming feedstock is larger in a fixed-bed reactor having a shell of a certain geometric size and configured (Bg) of the embodiments of the invention compared to a fixed-bed reactor of the same geometry. Thus, the new fixed-bed catalytic reactors that are configured (Gg) for embodiments of the invention The invention will have a higher sectional flow area rating than conventional units of the same size.Furthermore,conventional reactors can be upgraded from Gob 0 modified to conform to the configurations of the embodiments of the invention described in the present document.In this way, for conventional reactors in operation; For dehydrogenation reactors, redesigning/tooling according to embodiments of the invention can increase reactor productivity without leading mass formation and thus redesigning/tooling may lead to an increase in catalyst life for dehydrogenation reactors if the heat absorbed is kept constant. Endothermic reaction 5 and the catalyst bed size is reduced the average bed temperature will increase to provide the same heat for the original catalyst bed size.So in a given Jolie slog; In Ala the flow of the reactant is increased with the expectation of obtaining more products; The kinetics requires an increase in the cross-sectional area of the catalyst. This keeps the contact time the same (catalyst bed length/fluid velocity) at low throughput flow. An increase in cross-sectional area increases 0 heat storage volume of the catalyst bed and maintains kinetic contact time Gib Therefore the height to the Houdry reactor increases the cross-sectional area and keeps the contact time the same. This requires capital investment in parallel reactors. In most dehydrogenation plants; productivity increases with the vertical height of the Saal bed) and thus contact time change, but this increase is severely limited by the lack of space in the reactor and the ease with which the feed in these reactors can be increased by up to 750 over the design values.5 Near the end of the dehydrogenation batch cycle this design leads to overheating Heating

gal of the catalyst bed length as there is no reactant involved; which ultimately leads to 'lump Houdry mass 11000'; It is a dark red rough formation stalagmite like crude ruby however; Not surprisingly, decreasing the height of the catalyst bed increases the average temperature requirement of the solid and increases the injection of the reactant gas to keep the reaction rate constant. This paradox can only be solved by increasing the flow section area of the catalyst bed while increasing the throughput. The industry is unable to do so because the reactor geometry and size are ll although the operating economics suggest maximizing feedstock and throughput. There is a need to upgrade the design throughput rating of existing reactor vessels without resorting to Re-engineering of mechanical details.sale) Complete design in larger size requires increased 0 length of time and trial; dala when it comes to internal refractory 18" inner refractory liner is close to the artwork style. The proposed Wa reactor design innovatively changes the internal flow pattern and solves the above problems. After implementing embodiments of the invention in current industry operating units; Mass build-up is reduced and the reactor slog is able to raise productivity. And therefore; The unit can be upgraded to 5 parameters. It is obtained from the existing vascular design in a new plant. Embodiments of the invention can also save capital investment because when the embodiments are carried out in an industrial unit; They may require fewer parallel reactors to obtain a specific plate rating. Figure 11 and 1b show the fixed bed 10 reactor for hydrocarbon dehydrogenation; according to embodiments of the invention. fig. 71 and 1b show a front view of the fixed-bed reactor 10. The fixed-bed 0 reactor 10 is a catalytic reactor comprising catalyst bed 101 and catalyst bed 102 enclosed within wall 0. In embodiments of the invention; The catalyst bed 101 and catalyst bed 102 are two rectangular layers of equal size on either side of the fixed-bed reactor 10. Figure 5111b shows that the front view of wall 100 is round because the fixed-bed reactor 10 has a cylindrical shape. However; It should be noted that in embodiments of the invention; A fixed bed reactor 10 may have one or more walls 5 or more and may have other shapes such as a horizontal cylinder; vertical cylinder tank; rectangle tank; Oval Horizontal Tank» Horizontal Vertical Tank» Horizontal Capsule Tank and Vertical Capsule Tank.

Fixed-bed reactor 10 includes a feedstream inlet 103 (Lge) to divide the gas feedstream 109 and direct the gas feedstream 109 to the fixed-bed reactor 10. The fixed-bed 0 reactor also includes the jacket 104 (non-porous jacket); section (section 101 and section 02) for each of the catalyst bed 101 and catalyst bed 102, respectively.In this way, when the gas feed stream 109 flows through the inlet of the feed stream 103 to the fixed bed reactor 10, the feed stream lad 109 does not enter Catalyst bed 101 and catalyst bed 102 at section 1101 and section 102 respectively, which are the sections of each of the catalyst bed 101 and catalyst bed 102 closest to the feed stream inlet Yay 3. From that; the feed gas enters the catalyst bed 101 and the catalyst layer Catalyst 102 in Sections (AY) i.e. Section 101B and Section 102B. In embodiments of the invention, and constitutes catalyst layer 0 (eg JU catalyst layer 101 or catalyst layer 102) closest to the feed inlet (eg (Jill) Feed inlet 103 1/10 of the size of the catalyst bed (eg Section 1 and Section 1102) closest to the feed inlet (eg (Jaa) Feedstream inlet 103). in embodiments of the invention; The 10 static bed reactor does not include an inlet distributor. As mentioned above; The casing 104 can be made of metal such as stainless steel, carbon steels 5, ceramic material and mixtures thereof. In embodiments of cpl pal) the shell 4 may be one of the list consisting of: thermal arc roof reinforcing collar; SAE 310 STAINLESS STEEL OR COMPATIBLE BEND METAL » SAE 304 STAINLESS STEEL PLATE 1. COATING /

Polymeric paint that reduces deterioration from cyclic carbonation and oxidation-reduction environments. Since the jacket 104 covers the upper sections of the catalyst bed 101 and the catalyst bed 102 (section 0 101 and section 1102) so that the feed gas stream 109 does not enter the reactor fixed bed 10), the feed gas stream 109 does not enter the catalyst bed 101 and catalyst bed 102 in A direction parallel to the flow direction of the gas stream 109 through the inlet of the feed stream 103. Anmaa the feed gas stream 109 enters the catalyst bed 101 and the catalyst bed 102 in a lateral direction (as indicated by arrows 106) and/or obliquely (as indicated by arrows 110) On the flow direction of the gas feed stream (109) through the inlet of the feed stream 5 103. In other words, the feed gas stream 109 is transmitted to the wall 100 by means of the jacket 104 (non-porous thermal arc roof reinforcing collar) covering the top of the catalyst bed 101

and catalyst layer 102. In embodiments of the invention; The gas feed stream 109 enters the catalyst bed 101 and catalyst bed 102 through a shall which has downward slits to prevent catalyst particles from escaping. in embodiments of the invention; The gas feed stream 109 flows into the catalyst bed 101 and catalyst bed 102; As previously described; Wherein the gas feed stream 109 catalyst contacts the catalyst bed 101 and the catalyst bed ¢102 causing the hydrocarbons of the gas feed stream 109 (when the gas feed stream 109 contains paraffin Jie hydrocarbons) to dehydrogenate and form a gas product 111. The catalyst bed 101 and the catalyst bed are 102 is conditioned to flow a gas product 111 into the central chamber 107. The central chamber 7 is located between the catalyst layer 101 and the catalyst layer 102. Thereby; The central chamber 107 is configured to receive product gas flow 111 from catalyst bed 101 and catalyst bed 102.

0 The fixed bed reactor 10 may also include a manifold 108. As shown in Figure 1; in embodiments of the invention»; The manifold 108 is placed under the catalyst bed 101 and the catalyst bed 102 and is in fluid contact with the central chamber 107. In embodiments of the invention; The fixed-bed reactor 10 further comprises one or more of the outlets 112 in fluid contact with the manifold 108. The outlets 112 are shee for the flow of one or more gases from the manifold 108. In embodiments of the invention;

5 The fixed-bed reactor 10 has a first outlet 112 for air and a second outlet 112 for hydrocarbon exit, both of which are used in alternate cycles for dehydrogenation and decarburizing. The fixed-bed reactor 10 operates in cycles. in the first session; The gas feed stream 109 being a gas that includes hydrogenated hydrocarbons such as broyan, isobutane, butene, and isoointane. when

0 "The gas feed stream 109 is hydrogenated then it is product gas 111 which may include one or more olefins such as ethylene and propylene. The dehydrogenation process causes carbonization in the stationary reactor 10. dS) is the deposition of carbon in the reactor eg on the catalyst Which impairs the performance of the catalyst. Therefore, to maintain the efficiency of the dehydrogenation process, the Kreon in the second cycle is removed. In the second cycle, the gas feed stream 109 is the air that reacts with the Kreone to form the Kreon oxides

carbon oxides 25 (for example, carbon dioxide (CO2). Therefore, the gas product in the second cycle is gas containing carbon dioxide.

Figure 1] shows the fixed-bed reactor 10 in the direction in which the gas feed stream 109 enters the fixed-bed reactor 10 vertically downward. so; The casing 104 covers the top of the catalyst layer 101 and the catalyst layer 102 (sections 1101 and 1102) when the gas feed stream flow 109 entering the reactor is fixed layer 10 vertically downward and the casing 104 dag the gas feed stream 109 to flow Lal 5 (as indicated by arrows 106) to; or at an angle sala (WS) indicated by arrows 110) to; catalyst bed 101 and catalyst bed 102. In embodiments of the invention the jacket 104 with the wall 100 co-operate in directing the gas feed stream 109 to flow horizontally (as indicated by arrows 106) to ; or at an angle (LS) sala (as indicated by arrows 110) to ; catalyst bed 101 and catalyst bed 102. cally the jacket 104 dag the gas feed stream 109 flows along the wall 100 before the feed 0 stream enters the catalyst bed 101 and catalyst bed 102. Figure 1b shows the fixed bed reactor 10 in the direction where it enters Gas feed stream 109 fixed-bed reactor 10 Lila thus; The jacket 104 covers the side of the catalyst bed 101 and the catalyst bed 102 (sections 1101 and section 1102) when the feed gas flow 109) entering the reactor is fixed bed 10 laterally and the jacket 104 directs the feed gas stream 109 to flow vertically (as indicated by arrows 106 ) to or at an acute angle (WS) denoted by arrows 110) to catalyst bed 101 and catalyst bed 102. In embodiments of the invention the jacket 104 cooperates with the wall 100 to direct the gas feed stream 109 to flow vertically (WS) denotes it shares 106) to ; or at an angle (LS) sala indicated by arrows 110) to ; catalyst layer 101 and catalyst layer 102. Thus; The jacket 104 directs the flow of the gas feedstream 109 along wall 100 before the feedgas 109 enters catalyst bed 0 101 and catalyst bed 102. Figure 2 shows a side view of the fixed-bed reactor 10 for hydrocarbon dehydrogenation; according to the embodiments of the invention. Figure 3 shows Method 30 for dehydrogenation of hydrocrions in a fixed bed reactor; according to the embodiments of the invention. Method 30 can be performed using the fixed bed reactor 10. Method 30 may fas in the 300 meter; Cua may include the flow of a gas feed stream such as the gas feed stream 109 5 to a catalytic reactor Jo) eg.; fixed bed reactor 10) through feed inlet Jie feedstream inlet 103. The catalytic reactor may contain a combination of catalyst layers such as catalyst bed

1 and catalyst bed 102 shown in Figure 1. As implemented using the fixed bed 0 reactor, method 30 may include; In tank 301 direct the gas feed stream 109 away from the section of both catalyst bed 101 and catalyst bed 102 closest to the inlet of the feed stream 103 (section 1101 and section 1102). In embodiments of the invention” as implemented using a fixed-bed reactor 10), the routing is performed at least with the jacket 104 which is configured to cover part of both the catalyst bed assembly 101 and the catalyst bed 102 specifically Section 1101 and Section 1102. In Section 302; includes Method 30 Flow the gas feed stream 109 so that it enters both catalyst bed 101 and catalyst bed 102; not at section 1101 and section 1102 but at section AT (section 101b and section 2b) of both catalyst bed 101 and catalyst bed 102. When entering the gas feed stream 109 to

0 both catalyst layer 101 and catalyst layer 102; It enters in a direction that is not parallel to the flow direction of the gas feed stream 109 through the inlet of the feed stream 103. The feed gas stream 109 enters both the catalyst bed 101 and the catalyst bed 102 in a lateral direction (eo) eg.; As indicated by arrows 106) and/or italics (eg.; as indicated by arrows 110) indicates the direction of flow of the gas feedstream 109 through the inlet of the feedstream 103.

5 Pasteur 303 includes contacting the gas feed hydrocriones 109 with the catalyst bed 101 and catalyst bed 102 under sufficient reaction conditions to produce a gas product 111. When the gas feed 109 is a hydrocarbon; The Gas 111 product may include olefins such as ethylene and propylene. When the gas feed stream 109 is air; The gas 111 product may include carbon dioxide (002) oxides such as carbon dioxide.

0 in awful 304; Method 30 may include the flow of product gas 111 from catalyst bed 101 and catalyst bed 102 into a central chamber 107 (which is located between catalyst bed 101 and catalyst bed 102 and is prepared to receive product gas flow 111 from catalyst bed 101 and catalyst bed 102). For example, a gas product 111 flows through a thermal floor into the manifold 108. As shown in Figure 1, the manifold 108 is placed under the catalyst bed 101 and the catalyst bed 102

5 and is in fluid contact with the central chamber 107. In Al-Marie 306; Gas product 111 is discharged from fixed-bed reactor 10 through outlet 112.

Figure 4 shows Method 40 for reprocessing a fixed-bed Jolie for hydrocarbon dehydrogenation; according to the embodiments of the invention. Method 40 may include; In Terrible 400 Jolie determined a catalytic suitable for reprocessing according to embodiments of the invention. This catalytic reactor may include one or more walls; and a set of catalyst layers placed within the wall or I and a feed inlet conditioned to direct the flow of a feed gas stream into the catalytic reactor. Method 40 may also include; in awful 401; Adding one or more non-porous jackets to the catalytic reactor. The one or SST shall be a non-porous sheath (Liga) to cover part of each layer of the catalyst bed assembly so that when the gas feed stream flows through the feed inlet to the catalytic reactor; The gas feed stream does not enter the catalyst bed assembly at a section in each of the catalyst beds closest to the feed inlet. An Enmaa feed gas stream enters each catalyst bed

0 at another division for each catalyst layer. in embodiments of the invention; One or more non-porous casings and one or more wall bee of the gas feed stream so that the feed gas does not enter the catalyst bed assembly in a direction parallel to the direction of the gas feed stream flow through the feed inlet. INMAMA The gas feed stream enters each catalyst bed in a direction lateral and/or oblique to the direction of the gas feed stream flow through the feed inlet.

5 Embodiments of the invention can achieve an increase in the gas inlet cross-sectional area of the flow by using nearly the entire diameter of the bed while requiring minimal flow redistribution space at the inlet. Embodiments of the invention achieve 740% higher in design performance for a vessel designed as described in the present document than for a vessel of similar design and size in conventional reactors in conventional propane dehydrogenation service; And isobutane, isopentane, and butene-1. And compared to one layer

0 in single bowl design; The design of the embodiments of the invention can increase the catalyst volume by 1 and increase the gas flow area by 740. The typical total gas flow area through both existing layers is about 117.65 m2 and the catalyst bed outlet flow area remains fairly similar although embodiments of the present invention are Described with reference to the signs of Figure 3f

5 Fig. 4 However, it must be kept in mind that the process of the present invention is not limited to the particular sills and/or a particular arrangement of blocks shown in Fig. 3 and Fig. 4. By therefore; Availability of avatars

of the invention the functions specified herein using different boxes in a different order than in Fig. 3f

Figure 4. In the context of the present invention; Embodiments are described 20-1. Embodiment 1 is a catalytic reactor. The catalytic reactor includes one or more walls and a feed inlet oriented to direct the flow of a gas feed stream into the catalytic reactor. The Load catalytic reactor includes a set of catalyst layers placed inside the wall or AST where each catalyst layer contains a first end threaded from the feed inlet; And a second party placed further from the feeding entrance than the first party; And a middle part placed between the first party and the second party. The catalytic reactor also comprises one or more non-porous sheaths placed between the feed inlet and the catalyst bed assemblies and fitted to cover ohn The first end of each 0 bed assemblies includes the catalyst so that the feed gas entering the catalytic reactor is largely prevented from Entering each layer is a catalyst at the first end. Embodiment 2 is the catalytic reactor of Embodiment 1; In which two or more layers of catalyst are placed inside the wall. Embodiment 3 is the catalytic reactor of Embodiment 2 where the catalytic reactor has one non-porous sleeve Liga to cover ON each of the two catalyst layers. Embodiment 4 is the catalytic reactor according to either Embodiment 2 or 3; wherein the feed gas stream 5 does not enter the two catalyst beds in a direction parallel to the direction of flow of the feed gas through the feed inlet; Inmaa the gas feed stream enters each catalyst bed in a lateral and/or oblique direction to the flow direction of the gas feed stream through the feed inlet. Embodiment 5 is the catalytic reactor of any of Embodiments 1 through 4; The catalytic reactor includes a cylindrical vessel. Embodiment 6 is the catalytic reactor according to any of Embodiments 2 through 5 as it further comprises a central chamber between the two catalyst beds configured to receive 0 gas effluent from the catalyst beds. Embodiment 7 is the catalytic reactor of Embodiment 6; It also includes a manifold under the catalyst layers and in fluid contact with the central chamber. Embodiment 8 is the catalytic reactor of Embodiment 7; It also includes one or more outlets in fluid contact with the manifold and is prepared for the flow of one or more gases from the manifold. Embodiment 9 is the catalytic reactor of Embodiment 8; Where one or more of the gases includes 5 air, when operating the cycle of removal of creon 0660100712108. Embodiment 10 Ble for the catalytic reactor of embodiment 8; Where one or more of the gases includes a hydrocarbon gas at

Run the dehydrogenation cycle. Embodiment 11 is the catalytic reactor of any of Embodiments 1 through 10 in which one or more non-porous shells comprise a thermal arc roof reinforcing collar. Embodiment 12 is the catalytic reactor of any of Embodiments 1 through 10; where one or more of the non-porous casings comprise a curved sheet of stainless steel SAE 5 310 5. Embodiment 13 is the catalytic reactor of any of Embodiments 1 through 10; Where one or more non-porous casings comprise a curved SAE 304 .1 stainless steel plate with a polymeric coating/coating. Embodiment 14 is the catalytic reactor of any of Embodiments 1 through 13; where dag is the one or more non-porous sheaths the flow of the gas feed stream

Next to the walls before the gas feed stream entering the catalyst beds.

0 Embodiment 15 is a method for hydrocrion dehydrogenation. The method involves flowing a feed gas into a catalytic reactor through an Lge feed inlet to direct a feed gas flow into the catalytic reactor; Where the catalytic reactor contains one or more walls and a group of catalyst layers placed inside the wall “ST, where each catalyst layer includes a first party placed near the Adal inlet) and a second party placed further from the feed inlet from the first party” and ein Middle subject between the first party and the party

the second. The method for hydrocarbon dehydrogenation also includes directing the incoming gas feed stream into the catalytic reactor so that it is largely prevented from entering each catalyst bed at the first end; The shal is oriented using one or more non-porous sheaths placed between the feed inlet and the catalyst bed assembly. Embodiment 16 is the method of Embodiment 15 (it also includes a gas feed flow such that the feed gas does not enter the catalyst bed assembly in a direction parallel to the flow direction

gas feed stream through the feed inlet; Inmaa the gas feed stream enters each catalyst bed in a lateral and/or oblique direction to the flow direction of the gas feed stream through the feed inlet. Embodiment 17 is the method for embodiment 16; It also includes a gas product flow from the catalyst layers to a central chamber between the group of catalyst layers, and the central chamber is prepared to receive the gas product flow from the catalyst layers. Embodiment 18 is the method for Embodiment 17; It also includes product flow

5 The gas is through a manifold below the catalyst bed and in contact via the fluid with the central chamber.

Embodiment 19 is a catalytic reactor reprocessing method. The method includes providing a catalytic reactor with one or more walls; A feed inlet conditioned to direct a gas feed stream flow to the catalytic reactor. The load catalytic reactor comprises a set of catalyst layers placed inside the wall or ST where each catalyst layer includes a first end placed near the feed inlet; And a second party placed further from the feeding entrance than the first party; ejay is the middle subject between the first part and the second part. The method for retrofitting a catalytic reactor includes adding one or more non-porous jackets between the feed inlet and the catalyst bed group so that one or more non-porous jackets cover a portion comprising the first end of each layer of the catalyst bed group and this feed stream into the reactor is largely prevented The catalyst from entering each catalyst layer at the first end. Embodiment 20 is method 0 of embodiment 19) where one or more non-porous casings and one or more walls are prepared for the gas feed stream to enter all catalyst layers in a lateral and/or oblique direction on the feed gas stream flow direction through the feed inlet. Although Although embodiments of the present application and their advantages have been described in detail, it should be understood that many changes, substitutions and modifications may be made without departing from the spirit and scope of embodiments as defined in the appended claims. The current demand for embodiments of the process, machine, manufacture, composition of matter, methods, methods and steps described in the specification.As will be evident to a person of ordinary skill in the art from the above disclosure, the processes, machines, manufacture, combinations of matter, means, methods can be used or steps that currently exist or that will subsequently be developed to perform substantially the same function or achieve substantially the same result as the corresponding embodiments described in the present document. matter combinations, means, methods or steps within their scope. Sequence List: 5 3000 Flow the feed gas to the catalyst reactor through the inlet of the feed 1 direct the feed gas away from the section of each catalyst bed closest to the inlet of the feed gas

2 Flow of the gas feed stream so that each catalyst enters at another section for each of the catalyst layers 3 Contact of the hydrocarbons of the gas feed stream with the catalyst of the catalyst layers under sufficient reaction conditions to produce Jie “gle” olefins such as ethylene and propylene 4 The gaseous product flows from the catalyst layers into the chamber CENTRAL 305 Flow of Gaseous Product into Manifold 6 Discharge of Gaseous Product from Reactor 0 Identification of a Catalytic Reactor with a Group of Catalyst Beds and Suitable for Reprocessing 1 Add one or more jackets to the catalytic reactor to cover part of each layer in the group of catalyst beds so that when a feed stream flows gas through the feed inlet to the catalytic reactor; The 0 gas feed stream does not enter the catalyst bed group at the section of each of the catalyst layers closest to the feed inlet

Claims (7)

Claims 1 catalytic reactor comprising: wall; Lge feed inlet to direct the gas feed stream flow to the tcatalytic reactor where the gas feed includes hydrocrion; A group of catalyst beds placed inside the wall. Where each of the catalyst beds includes a first end positioned near the feed inlet; And a second party placed further from the feeding entrance than the first party; and a middle part placed between the first party and the second party; Where each catalyst layer contains a dehydrogenation catalyst, which “when in contact with the gas feed forms a gaseous product that includes a gaseous product containing 0 Wath olefins, hydrocarbon dehydrogenation, and a non-porous cover A nonporous cover placed between the feed inlet and the group of catalyst beds and prepared to cover a part that includes the first end of each layer of the group of catalyst beds so that the feed gas is divided and prevented from entering each catalyst layer bed at the first end 5 where the catalytic reactor is the fixed bed dehydrogenation reactor 2. The catalytic reactor according to claim 1 where two layers of catalyst 5 are placed inside the wall. 3 The catalytic reactor according to Clause 2, where the Gall catalytic reactor contains one nonporous cover prepared to cover part of each of the two catalyst beds. 4 the catalytic reactor according to claim 2 where the gas feed does not enter the catalyst beds in a direction parallel to the direction of the gas feed flow through the feed inlet; Rather, “the gas feed stream enters each catalyst ae 0 layer in a lateral and/or oblique direction to the direction of the gas feed flow through the feed inlet. 5 The catalytic reactor may be delivered in accordance with any of claims 1 to 3; Where the catalytic reactor includes a cylindrical vessel. 6. The catalytic reactor according to claim 2, as it also includes: a central chamber between the two catalyst beds prepared to receive the gas flowing from the catalyst beds 7. the catalytic reactor according to claim 6. It also includes: a manifold under the catalyst beds and in fluid communication 5 with the central chamber. 8 The catalytic reactor according to claim 7 also comprising: one or more outlets in fluid communication with the manifold 0 prepared for the flow of one or more gases from the manifold .20 9 The catalytic reactor may be delivered in accordance with any of claims 1 to 3; The nonporous covers include a roof shroud with a thermal arc .refractory arch 0. The Gy catalytic reactor of claim 1; Where the nonporous covers include a metal plate curved from stainless steel SAE 310 S. 5 11. catalytic reactor gall pursuant to claim 1; Where the non-porous casing includes a curved sheet of stainless steel of type SAE 304 L with polymeric coating/painting. 2. the catalytic reactor of claim 1; The non-porous casing directs the flow of the gas feed along the walls before the gas feed entering the catalyst beds. 3. A method for dehydrogenating a hydrocarbon, where the method includes: 15 A gas feed stream flows to a catalytic reactor according to Claim 1 through an Lge feed inlet to direct a gas feed stream flow Gas feed to the catalytic reactor Directing the incoming gas feed stream to the catalytic reactor so that it is prevented from entering each catalystbed at the first end; Where the routing is performed using the non-porous 0 casing placed between the feed inlet and the catalyst beds group Cus the gas feed touches the catalyst and the hydrocarbon is dehydrogenated to produce the olefin-containing gas product 4- The method according to Claim 13, Gus, also includes: the flow of the gas feed stream so that the gas feed stream does not enter the group of catalyst beds in a direction parallel to the direction of the gas feed stream flow gas feed through the feed inlet; Inmaa the gas feed stream enters each catalyst bed ise dish in a lateral and/or inclined direction to the direction of the gas feed flow through the feed inlet. 5. the method in accordance with claim 14; It also includes: SS JE product from the catalyst beds to a central chamber between the catalyst beds where the central chamber is the shee to receive the gas product flow from the catalyst beds 6- The method according to claim 15, which also includes: 10 Flow of the gas product through a manifold under the catalyst bed and in fluid communication with the central chamber. 7. The sale method is to supply a catalytic reactor where the method includes: providing a catalytic reactor where the catalytic reactor is a fixed bed dehydrogenation reactor which includes: a wall; Lge feed inlet to direct the flow of a gas feed stream containing hydrocarbon to the catalytic reactor A set of catalyst beds placed inside the walls where each layer includes 0 catalyst 560 catalyst on the tip of the first thread near the feed inlet; A second limb placed further from the feed entrance than the first limb »sing A middle thread between the first limb and the second limb; And updating the catalytic reactor to include a tnonporous cover Cua The improvement is made to the catalytic reactor by adding the nonporous cover between the feed inlet and the catalyst beds group so that the cover covers 5 non The porous Teja nonporous cover includes the first end of each layer of a group of layers — 2 4 — catalyst beds, and this feed stream inside the catalytic reactor was prevented from entering each dada catalyst bed at the first end dehydrogenation catalyst contains a catalyst bed each layer contains Cua catalyst produced by the removal of olefins, which forms inside it upon contact with the gas feed.” A gas product containing hydrogen olefins, hydrocarbon dehydrogenation. 8. the method in accordance with claim 17; Cun The nonporous cover and the wall are prepared for the gas feed flow to enter each catalyst bed in a lateral and/or oblique direction along the gas feed flow direction through the feed inlet. . ah 4 f ¥ x y 4 ak + + Fhe d ; iv, ha - Ya a aa “m een the bad aa 9 aa 1 khaa aa ala kr lwa \ rh a of ld. 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