CN215086990U - Radial reactor - Google Patents
Radial reactor Download PDFInfo
- Publication number
- CN215086990U CN215086990U CN202022938934.3U CN202022938934U CN215086990U CN 215086990 U CN215086990 U CN 215086990U CN 202022938934 U CN202022938934 U CN 202022938934U CN 215086990 U CN215086990 U CN 215086990U
- Authority
- CN
- China
- Prior art keywords
- reactor
- heat exchange
- radial
- exchange layer
- inner cylinder
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The application provides a radial reactor, the reactor includes inner tube, heat transfer layer, well section of thick bamboo, shell and annular space, the lateral wall of inner tube and well section of thick bamboo has a plurality of trompils respectively, it is a plurality of along radial reaction gas passageway to have in the heat transfer layer, the inner tube includes 3 to 6 large-scale lamellas and 0 to 6 small-size lamellas in the profile on radial cross-section, the figure that large-scale lamella and small-size lamella all obtained based on formula I is drawn.
Description
Technical Field
The utility model belongs to the field of chemical equipment, concretely relates to fixed bed catalytic reactor, especially radial reactor, this reactor is including having the inner tube lateral wall shape and the trompil shape of special optimization, can effectively improve the reaction rate of reaction, reduces the temperature gradient among the reaction process, has higher economic benefits.
Background
The fixed bed reactor can be divided into an axial reactor and a radial reactor according to the flowing mode, compared with the axial reactor, the radial reactor has the advantages of large height-diameter ratio, small bed pressure drop, short retention time of reactants in a catalyst bed, low operation cost, high production capacity, large scale and the like, and is widely applied to the fields of petrochemical industry, oil refining and the like. During operation of the radial reactor, the gas phase reactant material passes from the central flow path of the reactor through the catalyst reaction zone to react and product and unreacted material flow out of the annulus.
However, the radial reactor has the disadvantages that the radial reactor often has a relatively complex structure, wherein the flow regularity of the fluid is relatively complex, and the uneven radial flow velocity of the radial reactor causes uneven loading of the catalyst, deviation from the optimal operation condition, deterioration of the operation of the reactor, and the like; therefore, rectifying the flow in a radial reactor to distribute the flow as uniformly as possible is a technical key to the design of a radial reactor.
In addition, a strong exothermic reaction is often encountered in the chemical reaction process, and the radial reactor generates heat accumulation in a region with strong heat release or small heat exchange area so as to cause temperature runaway in the reactor, thereby causing the reduction of the conversion rate of the reaction and influencing the positive-to-differential ratio and selectivity of products, and in the most serious case, even possibly causing extremely serious carbon deposition and reactor failure.
Therefore, the radial reactors in the prior art still have problems to be solved such as low heat transfer efficiency, nonuniform radial gas reaction, and nonuniform flow in the actual chemical production. In view of the above problems, the inventors have developed a radial reactor in which the flow uniformity and temperature uniformity during the reaction are significantly improved by optimizing the shape of the flow channel, and the reaction efficiency is further improved, thereby solving the above problems that the prior art has difficulty in overcoming.
SUMMERY OF THE UTILITY MODEL
According to a first aspect of the present application, there is provided a radial reactor comprising, in radial order from inside to outside, an inner tube (1), a heat exchange layer (3), a middle tube (2), and an outer shell (5), an annulus (4) being provided between the middle tube (2) and the outer shell (5), the inner tube (1) being internally hollow with a first internal space, the heat exchange layer (3) being internally hollow with a second internal space, the inner tube (1), the heat exchange layer (3), the middle tube (2), the outer shell (5), and the annulus (4) having, in radial cross-section, a centrosymmetric shape and being concentric, sidewalls of the inner tube (1) and the middle tube (2) each having a plurality of openings, the heat exchange layer (3) having a plurality of reaction gas passages in radial direction therein; the profile of the inner cylinder (1) on the section along the radial direction comprises 3-6 large petals and 0-6 small petals, and the shapes of the large petals and the small petals are drawn based on a graph obtained by formula I:
in the formula I, LiRepresenting the side length of the initial equilateral triangle, L (n) representing the length of each line segment in the triangular fractal pattern drawn based on the initial equilateral triangle, 1<n≤5。
According to one embodiment of the first aspect of the present application, a first external space is enclosed between the inner drum (1) and the heat exchange layer (3), a second external space is enclosed between the heat exchange layer (3) and the middle drum (2), optionally the inner drum (1) itself encloses a third external space, at least one of the first external space, the second external space, the reaction gas channels of the heat exchange layer and optionally the third external space is filled with at least one material selected from the group consisting of: catalyst, filler, heat transfer material, solid or liquid reaction raw material and solid or liquid reaction auxiliary agent.
According to another embodiment of the first aspect of the application, the profile of the inner cylinder (1) in a cross section in the radial direction comprises 6 large lobes and 6 small lobes.
According to another embodiment of the first aspect of the application, the inner cylinder (1) has a sidewall with an open porosity of 15-50%. According to another embodiment of the first aspect of the application, the open porosity of the side wall of the central cylinder (2) is between 18 and 50%. According to another embodiment of the first aspect of the present application, the reactant gas channels of the heat exchange layer (3) occupy an area ratio of 10 to 50% on the side walls thereof.
According to another embodiment of the first aspect of the present application, the shape of the opening in the side wall of at least one of the inner cylinder (1) and the middle cylinder (2) is a shape based on formula I.
According to another embodiment of the first aspect of the present application, the top and/or bottom of the reactor is provided with a reactant inlet in fluid communication with the first interior space of the inner drum (1). According to another embodiment of the first aspect of the present application, the top and/or bottom of the reactor is provided with a product outlet, which is in fluid communication with the annulus (4); according to another embodiment of the first aspect of the present application, the top and the bottom of the reactor are provided with a heat exchange medium inlet and a heat exchange medium outlet, respectively, which are in fluid communication with the second inner space of the heat exchange layer (3), respectively.
According to another embodiment of the first aspect of the present application, the ratio between the radial diameter D of the radial reactor shell (5) and the radial reactor height H is between 1.0 and 10.0.
According to another embodiment of the first aspect of the application, the inner cartridge (1) further has one, two or three concentric annular parts.
According to a second aspect of the present application, there is provided a catalytic reaction process, carried out using the radial reactor of the present application, comprising the steps of:
gaseous raw materials are input into the inner cylinder (1), pass through the openings on the side wall of the inner cylinder (1), the reaction gas channel of the heat exchange layer (3) and the openings on the side wall of the middle cylinder (2), reach the annular space (4), are subjected to catalytic reaction in the process, and leave the reactor through the gap (4).
According to one embodiment of the second aspect of the present application, the heat exchange medium flows through the second inner space of the heat exchange layer (3) in the axial direction while exchanging heat with the outside of the heat exchange layer (3).
The structural design of the radial reactor developed in the present application and the reaction method using the reactor are described below in the detailed description section with reference to the drawings.
Drawings
The drawings show some of the designs of the present application and the prior art.
FIG. 1 shows a longitudinal cross-sectional view of a radial reactor according to one embodiment of the present application;
FIG. 2 shows a perspective view of a radial reactor according to one embodiment of the present application;
FIG. 3 shows a cross-sectional view of a radial reactor according to one embodiment of the present application;
4A-4D illustrate cross-sectional views of an inner barrel according to various embodiments of the present application;
FIG. 4E shows a cross-sectional view of an inner barrel of a comparative embodiment;
FIG. 5 shows a schematic view of an opening in the middle barrel 2 according to an embodiment of the present application;
FIG. 6 shows an enlarged schematic view of the opening of the inner cylinder 2 of FIG. 5;
FIG. 7 shows a graph obtained from a second iteration of formula I, according to an embodiment of the present invention;
fig. 8 shows a schematic diagram of a small petal based on a graph obtained from three iterations of formula I, according to an embodiment of the present invention;
fig. 9 shows a schematic diagram of a large petal based on a graph obtained by three iterations of formula I, according to an embodiment of the present invention.
Detailed Description
The "ranges" disclosed herein are in the form of lower and upper limits. There may be one or more lower limits, and one or more upper limits, respectively. The given range is defined by the selection of a lower limit and an upper limit. The selected lower and upper limits define the boundaries of the particular range. All ranges that can be defined in this manner are inclusive and combinable with each other, i.e., any lower limit can be combined with any upper limit to form a range. For example, ranges of 60-120 and 80-110 are listed for particular parameters, with the understanding that ranges of 60-110 and 80-120 are also contemplated. Furthermore, if the minimum range values 1 and 2 are listed, and if the maximum range values 3, 4, and 5 are listed, the following ranges are all contemplated: 1-3, 1-4, 1-5, 2-3, 2-4 and 2-5.
In this application, unless otherwise stated, the numerical range "a-b" represents a shorthand representation of any combination of real numbers between a and b, where a and b are both real numbers. For example, a numerical range of "0 to 5" indicates that all real numbers between "0 to 5" have been listed herein, and "0 to 5" is only a shorthand representation of the combination of these numbers.
In the present application, all embodiments and preferred embodiments mentioned herein may be combined with each other to form new solutions, if not specifically stated.
In the present application, all the technical features mentioned herein as well as preferred features may be combined with each other to form new technical solutions, if not specifically stated.
In the present application, all steps mentioned herein may be performed sequentially or randomly, if not specifically stated, but preferably sequentially. For example, the method comprises steps (a) and (b), meaning that the method may comprise steps (a) and (b) performed sequentially, and may also comprise steps (b) and (a) performed sequentially. For example, reference to the process further comprising step (c) means that step (c) may be added to the process in any order, for example, the process may comprise steps (a), (b) and (c), may also comprise steps (a), (c) and (b), may also comprise steps (c), (a) and (b), etc.
In the present application, the term "comprising" as used herein means open or closed unless otherwise specified. For example, the term "comprising" may mean that other components not listed may also be included, or that only listed components may be included.
In this application, the terms "inside", "outside", "over", "under" and the like, when used to describe the spatial relationship of a particular component or object with respect to other components or objects, mean that the former is inside, outside, above or below the latter, either directly in contact with each other or separated by a distance or spacing from a third component or object.
It is emphasized here that the embodiments shown in the figures and described below are merely some of the embodiments of the application, to which the scope of protection of the application is not limited. The scope of the present application is defined by the claims of the present application and may include any technical solutions within the scope of the claims, including but not limited to further modifications and substitutions of these specific embodiments.
In the present application, the term "cross-section" means a plane perpendicular to the axial direction of the reactor.
Some preferred reactors and processes of the present application are described hereinafter primarily based on the fischer-tropsch reaction, but it is emphasized that the reactions involved in the reactors and processes carried out using the reactors of the present application are not limited to the fischer-tropsch reaction, but can be used for any other reactions involving gas-solid phase interfacial interactions, and also provide technical improvements and benefits due to mass and heat transfer to these other processes, examples of which include chemical reactions such as ammonia synthesis, methanol synthesis, carbon monoxide shift, ethylene oxide synthesis, organic hydrogenation, oxidation, chlorination, sulfonation, alkylation, carbonylation, esterification, transesterification, catalytic isomerization, and chemical absorption of off-gases, etc.; bioengineering, such as biological fermentation, bacterial culture, etc. These reactions and processes may be exothermic or endothermic.
In the following embodiments of the present application, the terms "reactor", "radial reactor" and "radial flow reactor" are used interchangeably unless specifically indicated otherwise.
Fig. 1 and 2 show a schematic view of a radial reactor according to an embodiment of the present invention, comprising a housing 5, said housing 5 being adapted to enclose an inner space surrounding the reactor for performing a reaction, preferably a cylindrical housing, which may be, for example, a stainless steel cylindrical sealed pressure-bearing housing having a cylindrical shape. In order to clearly show the internal structure of the reactor, the top and bottom plates of the shell 5 are not shown in both fig. 1 and 2, in practice the shell 5 is sealed at its top with the top plate and at its bottom with the bottom plate. According to one embodiment of the present invention, one or more inlets are provided at the top or bottom of the housing 5 through which the gaseous reaction raw material is transported into the first inner space of the inner tube 1. According to a preferred embodiment, the inlet is provided at the top of the housing 5, and preferably at the center of the top plate cross-section, as indicated by the central arrow in FIG. 1, to deliver the gaseous reaction raw materials into the first interior space of the inner barrel 1. According to another embodiment of the present invention, one or more outlets are provided at the top or bottom of the housing 5 through which gaseous reaction products, unreacted gaseous starting materials, and by-product gases are transported from the annulus 4 to the outside of the reactor for subsequent product purification, recovery, and storage. According to a preferred embodiment the outlet is arranged at the top of the housing 5, and preferably at a position where the top plate cross section is close to the circumferential edge, more preferably aligned with the annulus 4 and evenly arranged along the midline of the annulus. According to one embodiment of the invention, gaseous reaction products, unreacted gaseous starting materials and by-product gases are conveyed out of the reactor from the annular space 4 through these outlets, as indicated by the arrows in the centre of fig. 1. According to a preferred embodiment of the invention, one or more, e.g. two, three, four, six, eight, ten, twelve, fifteen, eighteen, twenty-four, thirty outlets are provided at the top of the housing, all outlets being provided close to the circumferential edge in a centrally symmetrical manner, preferably in the top plate in a centrally symmetrical manner along the centre line of the annular gap 4. According to an embodiment of the present invention, the ratio of the radial diameter to the axial height of the housing 5 is 1:1.0 to 1:10.0, and may be, for example, within a range of values obtained by combining any two of the following values with each other: 1:1.0, 1:1.2, 1:1.5, 1:1.7, 1:1.8, 1:1.9, 1:2.0, 1:2.2, 1:2.5, 1:2.7, 1:2.8, 1:2.9, 1:3.0, 1:3.2, 1:3.5, 1:3.7, 1:3.8, 1:3.9, 1:4.0, 1:4.2, 1:4.5, 1:4.7, 1:4.8, 1:4.9, 1:5.0, 1:5.2, 1:5.5, 1:5.7, 1:5.8, 1:5.9, 1:6.0, 1:6.2, 1:6.5, 1:6.7, 1:6.8, 1:6.9, 1:7.7, 1:8.7, 1:8, 1:8.7, 1:8, 1:8.9, 1:8.7, 1:8, 1:8.9, 1:8, 1:8.9, 1:8, 1:8.8, 1:8, 1.8, 1:6.8, 1:8, 1.8, 1:8, 1.8, 1:8, 1.8, 1:8, 1.8, 1:8, 1.8, 1:8, 1.8, 1:8, 1.8, 1:8, 1.8, 1:8, 1.8, 1:8, 1.8, 1:8, 1.8, 1:8. According to one embodiment of the invention, the height of the outer reactor cylinder 5 may be 0.1 to 5 meters, such as 0.2 to 4 meters, or 0.5 to 3 meters, or 0.8 to 2 meters, or 1 to 1.5 meters, or may be within the range of any two of the above values in combination with each other.
As shown in fig. 1 to 3, the heat exchanger comprises an inner cylinder 1, a heat exchange layer 3 and a middle cylinder 2 in the outer shell 5 in the order from inside to outside in the radial direction, and an annular gap 4 is arranged between the middle cylinder 2 and the outer shell 5.
The inner cylinder 1 has a centrosymmetric cross-sectional shape and extends uniformly in the axial direction, i.e. has exactly the same cross-sectional shape over the entire axial direction.
The profile of the inner cylinder 1 on the cross section along the radial direction comprises 3 to 6 large petals and 0 to 6 small petals, and the shapes of the large petals and the small petals are drawn based on a graph obtained by formula I:
in the formula I, LiRepresenting the side length of the initial equilateral triangle, L (n) representing the length of each line segment in the triangular fractal pattern drawn based on the initial equilateral triangle, 1<n≤5。
According to an embodiment of the present invention, the drawing of the cross-sectional shape of the inner tube 1 according to the graph obtained by formula I comprises the following steps:
the first step involves selecting LiThe value of (d);
the second step comprises a step of measuring the length of the edge based on the length of the edgeiVirtual equilateral triangle, regular triangle based on drawing different grades of formula IA fractal pattern;
the third step comprises the steps of obtaining the outline of the inner cylinder 1 on the section along the radial direction based on the regular triangle fractal pattern obtained by iteration;
the fourth step is an optional step comprising scaling the contour of the obtained content 1 in a cross section in the radial direction equally.
According to a preferred embodiment of the present invention, L is selected based on actual conditionsiAfter the value of (2), the side length L is determinediIs referred to as an "initial triangle" in the present application. The applicant hereby states that the initial triangle described here is a figure that is used as a basis in an iterative process, and that no device or component having the initial triangle actually appears, but the shape of the inner cylinder 1 is based on the initial triangle and is designed after the iteration of formula I.
According to a preferred embodiment of the invention, the inner cylinder 1 has the cross-sectional shape shown in fig. 3, comprising six large petals arranged in a centrosymmetric manner, six small petals arranged in a centrosymmetric manner and two concentric annular parts.
According to an embodiment of the invention, each mini lobe comprises a triangular portion at the top, a rectangular portion connected to the triangular portion and optionally two or more diamond-shaped portions on either side of the mini lobe. The triangular part at the top is completely coincided with one regular triangle at the vertex of the regular triangle fractal pattern of the three iterations; the short side of the rectangular part is overlapped with the triangular part of the top part, and the long side extends along the radial direction of the cross section of the reactor; the optional diamond-shaped portion is disposed on either side of the mini lobe and extends from the side wall of the rectangular portion, the diamond having a first side overlapping a portion of the long side of the rectangular portion, a second side parallel to the first side, third and fourth sides parallel to each other, and an included angle (in acute angles) between the third and fourth sides and the first and second sides of 60 degrees.
According to an embodiment of the invention, the optional diamond-shaped portions are arranged in pairs on both sides of the small petals, e.g. one, two, three, four or five pairs of diamond-shaped portions are arranged in pairs on both sides of the small petals. According to another embodiment of the present invention, the pair of diamond-shaped portions has an interval between the outermost pair of diamond-shaped portions and the triangular portion of the top portion equal to the triangle side length of the triangular portion of the top portion, and an interval between each of the following diamond-shaped portions is also equal to the triangle side length of the triangular portion of the top portion. According to an embodiment of the present invention, the device comprises zero small petals. According to another embodiment of the present invention, three small petals are included. According to another embodiment of the present invention, the device comprises six small petals. According to one embodiment of the present invention, each of the small petals does not include a diamond-shaped portion thereon. According to one embodiment of the present invention, each of the small petals includes a pair of diamond-shaped portions thereon. According to another embodiment of the present invention, each of the small petals includes two pairs of diamond-shaped portions thereon. According to another embodiment of the present invention, each of the small petals includes three pairs of diamond-shaped portions thereon.
According to another embodiment of the present invention, each large petal comprises a triangular portion at the top, a rectangular portion connected to the triangular portion, and optionally two or more diamond-shaped portions located on both sides of the large petal in pairs. The top triangular part is an isosceles triangle with a vertex angle of 120 degrees and two sides with a length L (n), one short side of the rectangular part overlaps the fixed side of the isosceles triangle, the long side extends along the radial direction of the cross section of the reactor, the length of each optional diamond part is twice as long as the length of the two sides of the top triangular part, namely equal to 2L (n), the optional diamond parts are arranged on two sides of the rectangular part and extend from the side walls of the rectangular part, the first side of the diamond part overlaps a part of the long side of the rectangular part, the second side is parallel to the first side, the third side and the fourth side are parallel to each other, and the included angle (measured by an acute angle) between the third side and the fourth side and the first side and the second side is 60 degrees.
According to an embodiment of the present invention, the optional diamond-shaped portions are arranged in pairs on both sides of the large petal, for example, one, two, three, four or five pairs of diamond-shaped portions are arranged in pairs on both sides of the large petal. According to another embodiment of the present invention, the pair of diamond-shaped portions has an interval between the outermost pair of diamond-shaped portions and the triangular portion at the top equal to the side length of the diamond-shaped portion, and an interval between each of the following diamond-shaped portions is equal to the side length of the diamond-shaped portion. According to an embodiment of the present invention, the device comprises three large petals. According to another embodiment of the present invention, the device comprises six small petals. According to an embodiment of the present invention, each large petal does not include a diamond-shaped portion thereon. According to one embodiment of the present invention, each large petal includes a pair of diamond-shaped portions thereon. According to another embodiment of the present invention, each large petal comprises two pairs of diamond-shaped portions. According to another embodiment of the present invention, each large petal comprises three pairs of diamond-shaped portions.
According to some embodiments of the invention, the cross section of the inner cylinder 1 may also have one two or three concentric annular parts. According to one embodiment of the invention, the cross-section of each annular part is in the shape of a regular hexagon. According to another embodiment of the invention, the thickness of each ring-shaped part at each corner (i.e. the distance between the two walls of the ring-shaped part at this point) is equal to the side length of the diamond-shaped part in the large petal, and if there are multiple ring-shaped parts, the distance between adjacent ring-shaped parts at each corner is also equal to the side length of the diamond-shaped part in the large petal.
According to a preferred embodiment of the invention, the inner part of the cross-section of the innermost ring-shaped part is circular. According to one embodiment, the inner diameter of the circle is equal to the side length of the diamond on the large petal.
According to some embodiments of the present invention, all of the above-mentioned large petals, small petals and annular members extend longitudinally along the longitudinal axis of the reactor, and their walls enclose a first interior space in fluid communication with each other.
According to a preferred embodiment of the present invention, the inner cylinder 1 has a cross-sectional shape as shown in fig. 3, which is drawn based on the graph obtained by formula I described above. Specifically, the cross-sectional profile of the inner barrel 1, such as the cross-sectional profile of the inner barrel 1 shown in fig. 3, is obtained by:
the first step is to set the L of the initial equilateral triangleiWherein L isiMay be selected semi-empirically based on the process parameters of the target reactor that will be specifically employed (e.g., inlet flow, inlet velocity, inlet gas density, etc. that will be employed in the operation of the reactor). According to some embodiments of the present invention, the L can be completely based on the parameters of the inlet flow, the inlet speed, the inlet gas density, etc. that are finally needediThe choice is made so that the resulting cross-sectional area of the inner barrel 1 is adapted to the gas flowing in, as is the case, for example, in embodiments 1 and 6 of the present invention. According to other embodiments of the present invention, Li that has already been adopted is also directly selected, and after the cross-sectional profile of the inner tube 1 is drawn, the profile is scaled as needed, for example, as in the case of embodiments 2 to 5 of the present invention.
For example, according to one embodiment of the present invention, the reactor of the present invention has an inlet flow (expected to be used) of M kg/h, an inlet velocity of V M/h, and an inlet gas density of ρ kg/M3In this case, the value of parameter a may be determined based on the following formula II:
after the value of A is determined, the initial equilateral triangle L is determined based on the following equation IIiThe numerical value of (A):
thereby defining the dimensions of an equilateral triangle.
The second step is to determine LiThen, based on the side length as LiThe virtual equilateral triangle is used for drawing regular triangle fractal patterns with different grades based on a formula I, wherein n represents iteration times, and L (n) represents the length of each line segment on the periphery of the regular triangle fractal pattern. For example, FIG. 7 depicts the use of LiBased on the regular triangle fractal pattern drawn by the formula I and iterated twice, the periphery of the regular triangle fractal pattern can be seen to be formed by mutually zigzag connecting a plurality of line segments with the same length, and L (n) represents the length of each line segment on the periphery of the regular triangle fractal pattern. As another example, FIG. 8 shows the use of LiBased on a part of the triangular fractal pattern of the three iterations drawn by the formula I, it can be seen that the periphery of the triangular fractal pattern is also formed by mutually zigzag connecting a plurality of line segments with the same length, and l (n) represents the length of each line segment on the periphery of the triangular fractal pattern. The cross-sectional shape of the inner cylinder 1 shown in fig. 3 of the present invention is drawn based on the triangular fractal pattern of the three iterations shown in fig. 8.
The third step includes obtaining the profile of the inner cylinder 1 on a section in the radial direction based on the regular triangle fractal pattern obtained by iteration.
In particular, fig. 8 shows an embodiment in which small petals are obtained based on a triangular fractal pattern of three iterations. As can be seen in fig. 8, each mini lobe comprises a triangular portion at the top, a rectangular portion connected to the triangular portion, and optionally two or more diamond-shaped portions on either side of the mini lobe. See the embodiment shown in fig. 8, where the triangular portion of the top completely coincides with one regular triangle at the vertex of the triangular fractal pattern of the three iterations; the short side of the rectangular part is overlapped with the triangular part of the top part, and the long side extends along the radial direction of the cross section of the reactor; three pairs of diamond-shaped portions are disposed on either side of the mini lobe and extend from the side wall of the rectangular portion, the first side of the diamond overlapping a portion of the long side of the rectangular portion, the second side being parallel to the first side, the third and fourth sides being parallel to each other, and the third and fourth sides forming an angle (measured as an acute angle) of 60 degrees with the first and second sides. The three pairs of diamond parts are arranged on two sides of the small petal-shaped part in a paired mode, the interval between the outermost pair of diamond parts and the triangular part at the top is equal to the triangular side length of the triangular part at the top, and the interval between every two next diamond parts is also equal to the triangular side length of the triangular part at the top.
Fig. 9 shows an embodiment of obtaining large petals based on a triangular fractal pattern of three iterations. As can be seen in fig. 9, each large petal comprises a triangular portion at the top, a rectangular portion connected to the triangular portion, and optionally two pairs of diamond-shaped portions on either side of the large petal. The top triangular part is an isosceles triangle with a vertex angle of 120 degrees and two sides with a length L (n), one short side of the rectangular part overlaps the fixed side of the isosceles triangle, the long side extends along the radial direction of the cross section of the reactor, the side length of each diamond part is twice as long as the two sides of the top triangular part, namely equal to 2L (n), the diamond parts are arranged on two sides of the rectangular part and extend from the side walls of the rectangular part, the first side of the diamond part overlaps a part of the long side of the rectangular part, the second side is parallel to the first side, the third side and the fourth side are parallel to each other, and the included angle (measured by an acute angle) between the third side and the fourth side and the first side and the second side is 60 degrees.
According to one embodiment of the present invention, the optional diamond-shaped portions are disposed in pairs on both sides of the large petal, and two pairs of diamond-shaped portions are disposed in pairs on both sides of the large petal. According to another embodiment of the present invention, the pair of diamond-shaped portions has an interval between the outermost pair of diamond-shaped portions and the triangular portion at the top equal to the side length of the diamond-shaped portion, and an interval between the subsequent diamond-shaped portions is equal to the side length of the diamond-shaped portion.
As shown in fig. 9, the profile of the top triangle in the large lobe and the long side of the rectangular portion follow the shape of the lowest of the triangular fractal pattern of three iterations, but is opposite to this shape. The diamond shaped portions also partially follow a triangular fractal pattern of three iterations. FIGS. 4A-4D respectively show the cross-sectional shapes of inner barrel 1 having different configurations, where FIG. 4A is an inner barrel having six large petals, zero small petals, each of which has three pairs of diamond-shaped portions; FIG. 4B is an inner barrel with six large petals each having three pairs of diamonds and six small petals each having two pairs of diamonds; FIG. 4C is an inner barrel with six large petals, six small petals and an annular member, each of the large petals and the small petals not having a diamond shaped portion; fig. 4D is an inner barrel with three large petals and three small petals, each without a diamond-shaped portion. Fig. 4E shows another inner barrel cross-sectional shape that exhibits a conventional fractal structure similar to that of the present invention but not drawn based on formula I as in the present application.
For structures comprising annular members, it is also possible for the outer surface of the annular member to surround a third outer space, for example the space surrounded by the inner outer wall of the innermost annular member of fig. 3 and 4C, and the spaces surrounded by the outer walls of the plurality of annular members and the respective lobes. According to some embodiments of the invention, the third external space is not filled with any solid matter. According to further embodiments of the present invention, the third external space is filled with a solid substance, for example at least one material selected from the group consisting of: catalyst, filler, heat transfer material, solid reaction raw material and solid reaction auxiliary agent. The side wall of the inner cylinder 1 is provided with an opening. According to an embodiment of the present invention, the inner tube 1 has a plurality of openings thereon, which provide gas flow paths along the radial direction, so that the gas raw material entering the first inner space of the inner tube 1 from the inlet of the reactor top plate can flow through these openings along the radial direction to the heat exchange layer 3. According to an embodiment of the present invention, the open porosity of the outer wall (including the outer sidewall, and the inner sidewall-for the case including the annular member) of the inner tube 1 is 15 to 90%, or 18 to 60%, or 20 to 50%, or 22 to 45%, or 23 to 40%, or 25 to 38%, or 28 to 35%, or 30 to 33%, or the open porosity may be within a range of values obtained by combining any two of the above ranges of values; the pore size of each opening is in the range of 0.1-10 mm, preferably 0.5-8 mm, such as 0.8-5 mm, or 1-4 mm, or 2-3 mm, or the pore size of each opening may be within a range of values obtained by combining any two of the above ranges of values with each other. According to an embodiment of the invention, all openings are evenly distributed on the outer wall of the inner tube 1.
According to one embodiment of the invention, L is selectediOr by appropriate scaling after the cross-sectional configuration of the inner drum 1 has been drawn, so that the ratio of the area of said inner drum 1 in a plane perpendicular to the longitudinal axis of the reactor to the area of the space enclosed by said reactor shell in a plane perpendicular to the longitudinal axis of the reactor may be in the range of 5 to 70%, for example within the range of values which can be obtained by combining any two of the following values with each other: 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%.
As shown in fig. 3, a first external space is enclosed between the inner tube 1 and the heat exchange layer 3. According to some embodiments of the invention, the first outer space is not filled with any solid matter. According to further embodiments of the present invention, the first outer space is filled with a solid substance, for example at least one material selected from the group consisting of: catalyst, filler, heat transfer material, solid reaction raw material and solid reaction auxiliary agent. In the embodiment where the first external space is filled with the solid substance, the gas raw material contacts with the solid substance during the passage through the first external space, and undergoes a chemical reaction, a physical adsorption-desorption process, heat transfer, and the like.
Referring to fig. 3, a heat exchange layer 3 is provided outside the inner tube 1. According to some embodiments of the present invention, the interior of the heat exchange layer 3 is hollow, surrounding a second interior space. One or more heat transfer medium inlets for introducing a heat transfer medium into the heat exchange layer 3 to flow axially through the heat exchange layer 3 and one or more heat transfer medium outlets are provided in the top plate and the bottom plate of the casing 5, respectively. According to an embodiment of the invention, the heat transfer medium inlet is provided in the bottom plate of the housing 5 and the heat transfer medium outlet is provided in the top plate of the housing 5, according to a preferred embodiment of the invention, one or more, e.g. two, three, four, six, eight, ten, twelve, fifteen, eighteen, twenty-four, thirty inlets are provided in the bottom plate of the housing, all inlets being provided in the bottom plate in a centrosymmetric manner along the centerline of the heat exchange layer 3 in a centrosymmetric manner. According to a preferred embodiment of the invention, one or more, for example two, three, four, six, eight, ten, twelve, fifteen, eighteen, twenty-four, thirty outlets are provided in the top plate of the casing, all of which outlets are provided in the top plate in a centrally symmetrical manner along the centre line of the heat exchange layer 3 in a centrally symmetrical manner. During the reaction, the heat transfer medium flows axially in the heat exchange layer 3. According to an embodiment of the present invention, the heat exchange layer 3 is a circular ring structure, and the ratio of the inner diameter of the heat exchange layer 3 to the inner diameter of the outer shell 5 is 1:4 to 7:8, such as 1:3 to 5:6, such as 1:2 to 4:5, such as 2:3 to 3: 4. According to another embodiment of the present invention, the ratio of the thickness of the heat exchange layer 3 (the distance between the two side walls of the heat exchange layer 3 in the radial direction) to the inner diameter of the housing 5 is 1:100 to 1:7, such as 1:80 to 1:8, such as 1:60 to 1:9, such as 1:50 to 1:10, such as 1:40 to 1:12, such as 1:30 to 1:15, such as 1:20 to 1: 18. According to one embodiment of the present invention, a plurality of reactant gas channels are provided in the heat exchange layer 3, which reactant gas channels pass radially through the thickness of the heat exchange layer 3 on each horizontal cross section. According to an embodiment of the present invention, the aperture ratio of the outer wall (including the outer side wall and the inner side wall) of the heat exchange layer 3 is 15 to 90%, or 18 to 60%, or 20 to 50%, or 21 to 40%, or 22 to 30%, or 23 to 25%, or may be within a value range obtained by combining any two endpoints of the above value ranges; the size of the openings of each channel is 0.1-30 mm, preferably 0.5-28 mm, such as 0.8-25 mm, or 1-25 mm, or 2-24 mm, or 5-23 mm, or 8-22 mm, or 10-22 mm, or 12-21 mm, or 15-20 mm, or 18-20 mm, or may be within the range of any two of the above values in combination with each other. According to an embodiment of the invention, the openings of all channels are evenly distributed on the outer wall of the inner cylinder 1. According to one embodiment of the present invention, the size and shape of the channels in the heat exchange layer 3 are the same as the shape of the openings in the side wall of the inner tube 1, for example, they are circular. According to an embodiment of the utility model, every passageway aligns with an trompil on the inner tube 1 lateral wall for the material can pass through a passageway in heat transfer layer 3 through not any direction change after passing through an trompil on the inner tube 1 lateral wall. According to another embodiment of the present invention, each channel is staggered with respect to the opening in the side wall of the inner barrel 1, so that the material, after passing through an opening in the side wall of the inner barrel 1, needs to pass through a channel in the heat exchange layer 3 at least partially after undergoing a change of direction. According to some embodiments of the invention, the channel is not filled with any solid matter. According to further embodiments of the present invention, the channels are filled with a solid substance, for example at least one material selected from the group consisting of: catalyst, filler, heat transfer material, solid reaction raw material and solid reaction auxiliary agent. For embodiments in which the channels are filled with a solid material, the gas feed contacts the solid material during passage through the channels and undergoes chemical reactions, physical adsorption-desorption processes, heat transfer, and the like.
As shown in fig. 3, a second external space is enclosed between the heat exchange layer 3 and the inner tube 2. According to some embodiments of the invention, the second outer space is not filled with any solid matter. According to further embodiments of the present invention, the second outer space is filled with a solid substance, for example at least one material selected from the group consisting of: catalyst, filler, heat transfer material, solid reaction raw material and solid reaction auxiliary agent. In the embodiment where the second external space is filled with the solid substance, the gas raw material contacts with the solid substance while passing through the second external space, and undergoes a chemical reaction, a physical adsorption-desorption process, heat transfer, and the like.
Referring to fig. 3, a middle tube 2 is disposed outside the heat exchange layer 3. According to some embodiments of the present invention, the interior of the middle barrel 2 is not hollow, but the side wall of the middle barrel 2 has an opening. According to an embodiment of the present invention, the middle cylinder 2 is a circular ring structure, and the ratio of the inner diameter of the middle cylinder 2 to the inner diameter of the outer shell 5 is 1:3 to 7:8, such as 2:5 to 5:6, such as 1:2 to 4:5, such as 2:3 to 3: 4. According to another embodiment of the present invention, the thickness of the middle barrel 2 (the distance between the two side walls of the middle barrel 2 in the radial direction) is 0.1-10%, such as 0.2-9%, such as 0.4-8%, such as 0.5-7%, such as 0.6-6%, such as 0.7-5%, such as 0.8-4%, such as 0.9-3%, such as 1-2% of the inner diameter of the outer shell 5. According to an embodiment of the present invention, as shown in fig. 5, the openings are uniformly distributed in the side wall of the middle cylinder 2, for example, the opening ratio on the outer wall (including the outer side wall and the inner side wall) of the middle cylinder 2 may be 10 to 90%, or 11 to 70%, or 12 to 60%, or 13 to 50%, or 14 to 40%, or 15 to 30%, or 16 to 25%, or 17 to 24%, or 18 to 20%, or may be within a numerical range obtained by combining any two endpoints of the above numerical ranges. According to an embodiment of the present invention, the opening area of each opening may be 0.01-4000 square millimeters, such as 0.1-3000 square millimeters, or 1-2500 square millimeters, or 5-2000 square millimeters, or 10-1800 square millimeters, or 80-1500 square millimeters, or 100-1200 square millimeters, or 200-1000 square millimeters, or 400-800 square millimeters. According to one embodiment of the invention, all openings are evenly distributed on the outer wall of the middle tube 2. According to an embodiment of the present invention, the shape of the opening on the middle barrel 2 is the same as the shape of the opening on the side wall of the inner barrel 1, for example, both are circular. According to the utility model discloses an embodiment, every trompil aligns with an open channel of heat transfer layer 3 on well section of thick bamboo 2 for the material can pass through the opening in well section of thick bamboo 2 through any direction change after passing through a passageway in heat transfer layer 3. According to another embodiment of the present invention, each opening of the middle tube 2 is staggered with an open channel of the heat exchange layer 3, so that the material needs to be at least partially changed in direction to pass through the opening of the middle tube 2 after passing through a channel of the heat exchange layer 3.
According to a preferred embodiment of the present invention, the shape of the openings or channels on the side walls of the inner tube 1, the heat exchange layer 3 and the middle tube 4 can be circular or other shapes. According to a preferred embodiment of the present invention, the shape of the opening in the sidewall of the inner cylinder 1 is circular or the shape shown in fig. 1. According to another preferred embodiment of the present invention, the shape of the channels in the heat exchange layer 3 is circular. According to another embodiment of the invention, all the openings are evenly distributed on the outer wall of the middle tube 2, as shown in fig. 5. Preferably, the shape of the opening on the side wall of the middle cylinder 2 is an interrupted circular ring. Fig. 6 shows an enlarged view of an opening in the middle tube 2, said opening being in the shape of a discontinuous circular ring having an inner diameter of 5-30 mm, such as 8-28 mm, or 10-26 mm, or 12-25 mm, or 15-24 mm, or 18-22 mm, or 20-21 mm, or in a range of values where any two of the above ranges of values are combined; the outer diameter of the ring may be 10-50 mm, such as 20-48 mm, or 25-46 mm, or 28-44 mm, or 30-43 mm, or 35-42 mm, or 38-41 mm, or may be within any range of values where any two of the above ranges are combined. The ring may be divided into a discontinuous circular ring shape by three or six discontinuities (six as shown in fig. 5 and 6), each discontinuity may be in the form of a segment extending across the ring in a radial direction of the circular ring shape. According to an embodiment of the present invention, the area ratio of the discontinuous portion may be, for example, 5 to 40%, or 10 to 35%, or 15 to 34%, or 20 to 30%, or 25 to 28%, or may be within a numerical range obtained by combining any two endpoints of the above numerical ranges, based on the total area of the whole circular ring shape.
Fig. 1 shows a pattern of gas flow in a reaction gas in a catalytic reaction process according to an embodiment of the present invention. In this embodiment, a solid substance is filled in a first outer space between the inner tube 1 and the heat exchange layer 3 and a second outer space between the heat exchange layer 3 and the inner tube 2, and for the fischer-tropsch reaction, the filled solid substance is a catalyst for the fischer-tropsch reaction, such as an iron-based catalyst, a cobalt-based catalyst, a ruthenium-based catalyst, a nickel-based catalyst, or a catalyst containing a combination of two or more of iron, cobalt, ruthenium, and nickel. During the reaction, the gaseous feed (syngas, i.e. a mixture of hydrogen and carbon monoxide) is introduced into the first interior space of the inner barrel 1 from one or more inlets in the top plate of the outer shell 5, preferably one inlet located in the center of the top plate, and flows in a radial direction at each opening. For embodiments in which the inner barrel 1 comprises annular members and the outer side wall of each annular member encloses a "third outer space", it is also possible for the gaseous raw materials to pass radially through the third outer space enclosed by said annular members and then to be conveyed radially outwards. During the process of passing through the first and second outer spaces, the gas contacts with the solid material (such as the catalyst for fischer-tropsch reaction) filled in the first and second outer spaces, and fischer-tropsch catalytic reaction is carried out to form hydrocarbon products, byproducts (such as non-target hydrocarbons, oxygenates, etc.) and water vapor. The gas flow is in heat exchange with the heat exchange medium flowing axially in the heat exchange layer 3 in the process of passing through the channel in the heat exchange layer 3, the heat generated by the reaction is taken away, the heat transfer medium carrying waste heat leaves the reactor at the top of the reactor, and after the waste heat is recovered by the heat exchanger outside the reactor, the waste heat can be input into the heat exchange layer 3 from the bottom of the reactor for recycling. The product mixture gas stream formed after the above-described catalytic reaction, which comprises hydrocarbon products, by-products (e.g., non-target hydrocarbons, oxygenates, etc.) and water vapor, enters the annulus 4 through the openings of the tundish 2 and rises within the annulus 4 as indicated by the arrows to the top of the reactor where it is discharged. The product mixture gas stream exiting the gas outlet may be collected, stored, purified, derivatized, further reacted, further fractionated, conveyed to waste gas treatment, or discharged directly as desired.
According to an embodiment of the present invention, during the catalytic reaction, the flow of the raw material gas flow inputted into the inner barrel 1 can be properly adjusted according to the capacity of the reactor and the specific process requirements, for example, can be 0.1 ml/s to 10 l/s. The entry temperature of the feed gas stream is 150-280 deg.C, such as 190-220 deg.C, or 195-210 deg.C, and the pressure in the reactor can be maintained at 1.0-8.0MPa, such as 2.0-4.0MPa, such as 2.2-2.5 MPa.
According to the utility model discloses an embodiment, one or more designs in the roof of reactor, bottom plate and the inside inner tube of reactor, heat transfer layer and well section of thick bamboo are for can dismantling the form to the installation of reactor, maintenance and the packing and the change of catalyst. For example, in a preferred embodiment, at least one of the top plate and the bottom plate is designed to be detachable, the catalyst is filled by pumping when the catalyst is filled, and the top sealing plate is hermetically connected with the side wall of the catalytic reaction zone (i.e. the area filled with the catalyst) after the catalyst is filled; when the catalyst is removed, the top sealing plate is removed and then the catalyst is removed by a catalyst remover.
In some embodiments of the invention, other devices, such as valves, flow meters, thermometers, pressure gauges, heat exchange devices, baffles, flanges, threads, pins, fins, and any combination thereof, may be added to the reactor, either externally or internally, as desired, to one or more components of the reactor.
Without wishing to be bound by any particular theory, in the prior art to promote heat and mass transfer in radial reactors and to reduce flow dead zones throughout the reactor, it is generally desirable for the cross-section of the inner barrel to have a shape that is as simple and uniform as possible, and to minimize structures such as corners that may introduce dead zones. Thus, the conventional wisdom of the prior art is that optimum mass and heat transfer can be achieved with a circular or simplest radial cross-sectional shape for the inner barrel 1. Similarly, the conventional wisdom of the prior art also holds that the simplest aperture shapes on the inner or middle barrel side walls can achieve optimal mass and heat transfer effects.
However, contrary to these conventional beliefs of the prior art, applicants have unexpectedly discovered in their research that by employing a specifically defined cross-sectional shape of the inner barrel, a design of the shape of the openings in the sidewall of the middle barrel, or a combination of both, excellent reduction of dead space, and overall improvement of mass and heat transfer in various regions within the reactor are achieved, where the design of the structure and the mass and mass transfer improvement effect are completely contrary to the conventional beliefs of the prior art. When the reactor of the utility model is used for carrying out catalytic reaction such as Fischer-Tropsch reaction, the pressure drop in the reactor is obviously reduced, the retention time is shortened, the operation cost is reduced, the purpose of increasing the contact surface of the feed gas and the catalyst is achieved on the premise of not increasing the overall shape and size of the radial reactor, the reaction is more sufficient, and the reaction rate is improved; the better heat transfer effect improves the temperature management in the reaction system; better mass transfer improves the flow uniformity of the gas stream. In addition, the reactor of this application can carry out convenient scaling, can carry out the upsizing very easily and be applied to industrial production or can be based on the utility model discloses carry out very convenient transformation and upgrading to the current equipment of chemical enterprise.
Examples
The preferred embodiments of the present invention are specifically illustrated in the following examples, but it should be understood that the scope of the present invention is not limited thereto.
Example 1: use the reactor of the utility model to carry out the Fischer-Tropsch reaction
In this example 1, a radial reactor as shown in FIG. 2 was constructed, the inner diameter of the reactor shell 5 being 1000mm and the height being 1000 mm. The inner barrel 1 of the reactor has the structure shown in fig. 3, and comprises six large petals, six small petals and two annular parts, and the shape of the inner barrel is drawn based on formula I as described in the above specification. The respective dimensions are as follows: the length of the large petal-shaped portion from the innermost end to the outermost end was 130mm, the width (of the rectangular portion of the large petal-shaped portion) was 22.5mm, the top angle was 120 degrees, and two pairs of diamond-shaped protruding members each having a side length of 26mm were provided.
The total length of the small petal-shaped portions from the innermost end to the outermost end was 65mm, and the width (of the rectangular portions of the small petal-shaped portions) was 13 mm. The apex angle is 60 degrees. Two pairs of diamond-shaped projections were provided, each diamond-shaped projection having a side length of 13 mm.
Possess 2 annular channel, the radius of central circle is 29mm, from inside to outside, the passageway wall that three hexagon in total constituteed, the radius of three hexagon inscription circle is respectively from inside to outside: 58mm, 87mm, 116 mm.
The sectional area of the gas passage of the inner cylinder 1 is 745cm2。
The inner cylinder 1 is provided with circular holes with the diameter of 2mm on all side walls, the hole opening rate is 25%, the thickness of the heat exchange layer 3 is 50mm, the radius of the central position of the heat exchange layer is 335mm, the penetrating channel for gas circulation in the heat exchange layer is a circular channel with the diameter of 20mm, the hole opening rate of the heat exchange layer is 23.86% (based on the section of the central position), the thickness of a circular annular gap is 60mm, the thickness of the middle cylinder 2 is 2mm, the side wall of the middle cylinder 2 is provided with the holes as shown in figure 6, the holes are in the form of discontinuous circular rings, the inner diameter of each discontinuous circular ring is 20mm, the outer diameter of each discontinuous circular ring is 40mm, the distance between each partial sector is 3.2mm, the hole opening rate is about 16%, and the diameter of the central line in the sectional view of the middle cylinder 2 is 435 mm. The catalyst is filled in the gaps among the components except the annular gap 4 and the channels of the heat exchange layer, the adopted catalyst is a cobalt-based Fischer-Tropsch synthesis catalyst prepared by adopting an impregnation method according to the prior art, and a carrier Al2O3Has a pore volume of about 0.5mL/g and a specific surface area of about 150m2The catalyst has an average pore diameter of about 13nm per gram. The molar ratio of CO to H2The synthesis gas of 1:1 was first heated to 210 c, then introduced into the inner tube 1 from the inlet at the top center at a flow rate of 377kg/h (gas velocity of 0.1m/s), and then flowed and reacted in the reactor as shown by the arrow of fig. 1, with a feed gas pressure of 2.2 MPa. During the reaction, cooling water flows through the heat exchange layer, and the temperature in the reactor is maintained at 230 +/-3 ℃.
Five temperature sensors are uniformly arranged at different heights of the inner cylinder wall and the middle cylinder wall in the reactor respectively, and the average value of the five temperature sensors is used as the average temperature of the inner cylinder and the middle cylinder. The reaction product was sampled and the CO content thereof was characterized by gas chromatography, from which the CO conversion in the reactor was calculated. The results are summarized in Table 1 below.
Example 2: use the reactor of the utility model to carry out the Fischer-Tropsch reaction
In this example 2, the conditions and steps of example 1 were repeated except that an inner tube including only six large petals shown in fig. 4A was used, and the inner tube was increased by 23% in an equal proportion to example 1 to make the internal space in the cross section equal to example 1. The temperature stability and CO conversion were characterized in the same manner as in example 1 and the results are summarized in table 1 below.
Example 3: use the reactor of the utility model to carry out the Fischer-Tropsch reaction
In this example 3, the conditions and steps of example 1 were repeated except that an inner cylinder including six large petals and six small petals shown in fig. 4B was used, and the inner cylinder was enlarged by 8% in an equal proportion to example 1 so that the inner space in the cross section thereof was equal to example 1. The temperature stability and CO conversion were characterized in the same manner as in example 1 and the results are summarized in table 1 below.
Example 4: use the reactor of the utility model to carry out the Fischer-Tropsch reaction
In this example 4, the conditions and steps of example 1 were repeated except that an inner cylinder including six large petals, six small petals and one ring shown in fig. 4C was used, and the inner cylinder was increased by 33% in an equal proportion to example 1 so that the inner space in the cross section thereof was equal to example 1. The temperature stability and CO conversion were characterized in the same manner as in example 1 and the results are summarized in table 1 below.
Example 5: use the reactor of the utility model to carry out the Fischer-Tropsch reaction
In this example 5, the conditions and steps of example 1 were repeated except that the inner tube including three large petals and three small petals shown in fig. 4D was used, and the inner space in the cross section thereof was made equal to example 1 by increasing the inner tube by 60% in an equal proportion to example 1. The temperature stability and CO conversion were characterized in the same manner as in example 1 and the results are summarized in table 1 below.
Comparative example 1:
this comparative example was carried out under the same conditions and procedures as in example 1, with the only difference that the cross-section of the inner cylinder was circular, the cross-sectional area of the circular inner cylinder being equal to the cross-sectional area of the inner cylinder of example 1. The temperature stability and CO conversion were characterized in the same manner as in example 1 and the results are summarized in table 1 below.
Comparative example 2:
this comparative example was carried out under the same conditions and procedures as in example 1, with the only difference that the heat exchange layer was omitted, and the space of the heat exchange layer was occupied by an equal volume of catalyst. The temperature stability and CO conversion were characterized in the same manner as in example 1 and the results are summarized in table 1 below.
Comparative example 3:
in this comparative example 3, the conditions and steps of example 1 were repeated except that the shape shown in fig. 4E, which is a conventional fractal shape but does not satisfy the definition of formula I, was used. The cross-sectional area was made equal to that of example 1 by scaling. The temperature stability and CO conversion were characterized in the same manner as in example 1 and the results are summarized in table 1 below.
Example 6:
in this example 6, the conditions and steps of example 1 were repeated except that the shape of the opening on the side wall of the middle tube 2 was changed from the shape shown in fig. 6 to a circular shape having the same area, and the opening ratio of the middle tube 2 was not changed with respect to example 1. The temperature stability and CO conversion were characterized in the same manner as in example 1 and the results are summarized in table 1 below.
Table 1: temperature stability and catalytic reaction results of examples 1-6 and comparative examples 1-3
| Mean temperature on middle barrel | Temperature difference between inner tube and middle tube | Conversion of CO | |
| Example 1 | 230 |
3℃ | 45.6 |
| Example 2 | 235 |
5℃ | 44.1 |
| Example 3 | 229℃ | 4.2℃ | 44.8 |
| Example 4 | 228 |
4℃ | 45.0 |
| Example 5 | 234℃ | 4.8℃ | 42.8 |
| Comparative example 1 | 232 |
3℃ | 34.5 |
| Comparative example 2 | 239℃ | 10℃ | 35.5 |
| Comparative example 3 | 242℃ | 12℃ | 32 |
| Example 6 | 230 |
3℃ | 42.6 |
Claims (8)
1. A radial reactor comprises an inner cylinder (1), a heat exchange layer (3), a middle cylinder (2) and an outer shell (5) in sequence from inside to outside in the radial direction, wherein an annular gap (4) is arranged between the middle cylinder (2) and the outer shell (5), the inner cylinder (1) is hollow inside and has a first inner space, the heat exchange layer (3) is hollow inside and has a second inner space, the inner cylinder (1), the heat exchange layer (3), the middle cylinder (2), the outer shell (5) and the annular gap (4) have centrosymmetric shapes and are concentric on a radial section, the side walls of the inner cylinder (1) and the middle cylinder (2) are respectively provided with a plurality of openings, and a plurality of reaction gas channels along the radial direction are arranged in the heat exchange layer (3);
the inner cylinder (1) is characterized in that the profile of the cross section of the inner cylinder in the radial direction comprises 3-6 large petals and 0-6 small petals, and the shapes of the large petals and the small petals are drawn based on a graph obtained by a formula I:
in the formula I, LiRepresenting the side length of the initial equilateral triangle, L (n) representing the length of each line segment in the triangular fractal pattern drawn based on the initial equilateral triangle, 1<n≤5。
2. The radial reactor according to claim 1, characterized in that the profile of the inner cylinder (1) in a cross section in the radial direction comprises 6 large lobes and 6 small lobes.
3. The radial reactor of claim 1,
the opening rate of the side wall of the inner barrel (1) is 15-50%;
the opening rate of the side wall of the middle barrel (2) is 15-50%; and is
The reaction gas channel of the heat exchange layer (3) occupies 10-50% of the area of the side wall.
4. The radial reactor according to claim 1, characterized in that the shape of the opening in the side wall of at least one of said inner (1) and intermediate (2) cylinders is discontinuous circular.
5. The radial reactor of claim 1,
the top and/or bottom of the reactor is provided with a reactant inlet which is in fluid communication with the first inner space of the inner drum (1);
the top and/or bottom of the reactor is provided with a product outlet in fluid communication with the annulus (4); and is
The top and the bottom of the reactor are respectively provided with a heat exchange medium inlet and a heat exchange medium outlet, and the heat exchange medium inlet and the heat exchange medium outlet are respectively communicated with the second inner space of the heat exchange layer (3) in a fluid mode.
6. The radial reactor according to claim 1, wherein the ratio between the radial diameter D of the radial reactor shell (5) and the radial reactor height H is between 1.0 and 10.0.
7. The radial reactor according to claim 1, characterized in that the inner cylinder (1) also has one, two or three concentric annular parts.
8. The radial reactor according to claim 1, wherein the ratio of the cross-sectional area of the inner cylinder (1) in a plane perpendicular to the longitudinal axis of the reactor to the cross-sectional area of the space in the outer shell (5) in a plane perpendicular to the longitudinal axis of the reactor is 10-70%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022938934.3U CN215086990U (en) | 2020-12-10 | 2020-12-10 | Radial reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022938934.3U CN215086990U (en) | 2020-12-10 | 2020-12-10 | Radial reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN215086990U true CN215086990U (en) | 2021-12-10 |
Family
ID=79263486
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022938934.3U Active CN215086990U (en) | 2020-12-10 | 2020-12-10 | Radial reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN215086990U (en) |
-
2020
- 2020-12-10 CN CN202022938934.3U patent/CN215086990U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US5405586A (en) | Radial flow heat exchanging reactor | |
| RU2361657C2 (en) | Fixed-bed catalytic reactor | |
| CN105032305B (en) | A kind of new radial direction plate-type reactor | |
| RU2398733C2 (en) | Converter system with maximum reaction speed for exothermic reactions | |
| RU2279307C2 (en) | Pseudo-isothermal catalytic reactor and the lumped heat exchanger for realization of the exothermal and endothermic chemical reactions | |
| US8071059B2 (en) | Chemical reactor | |
| US4341737A (en) | Apparatus for carrying out catalytic exothermic and endothermic high-pressure gas reactions | |
| EP2249954B1 (en) | Catalytic reactor | |
| KR101794495B1 (en) | Device for distributing feed and recovering effluents in a radial bed catalytic reactor | |
| WO2018114900A1 (en) | Oxidative dehydrogenation (odh) of ethane | |
| US7381851B2 (en) | Method for producing formaldehyde | |
| CN103990420A (en) | Multitubular fixed bed reactor and application thereof | |
| CN215086990U (en) | Radial reactor | |
| WO2009123151A1 (en) | Plate type reactor, manufacturing method therefor, and reaction product manufacturing method using the plate type reactor | |
| AU2016299704A1 (en) | Tube isothermal catalytic reactor | |
| CN112604609A (en) | Radial reactor and catalytic reaction method using same | |
| US20170361312A1 (en) | Engineered inert media for use in fixed bed dehydrogenation reactors | |
| US20200384431A1 (en) | Adiabatic axial flow converter | |
| CN107519823B (en) | A kind of subregion radial reactor | |
| US20060171868A1 (en) | Pseudo-isothermal radial reactor | |
| CN204933424U (en) | A kind of novel radial plate-type reactor | |
| CN102463076A (en) | Novel external modularized grid used for radial bed reactor | |
| JP6088120B2 (en) | Plate type reactor, method for producing the same, and method for producing a reaction product using the reactor | |
| RU2371243C1 (en) | Catalytic reactor | |
| RU2243028C1 (en) | Reactor for a catalytic dehydrogenation of hydrocarbons |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |