CN116648304A - fixed bed reactor - Google Patents
fixed bed reactor Download PDFInfo
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- CN116648304A CN116648304A CN202180086162.XA CN202180086162A CN116648304A CN 116648304 A CN116648304 A CN 116648304A CN 202180086162 A CN202180086162 A CN 202180086162A CN 116648304 A CN116648304 A CN 116648304A
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- fixed bed
- bed reactor
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- inlet baffle
- inlet
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
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Abstract
The present invention provides a fixed bed reactor comprising: a pipe for introducing a gas-liquid two-phase flow from an upper portion of the fixed bed reactor into an interior; and an inlet baffle plate disposed in the fixed bed reactor so as to face the inlet of the pipe, wherein the inlet baffle plate is a flat plate disposed horizontally, the inlet of the pipe is disposed directly above the center position of the inlet baffle plate, a shielding portion is vertically disposed on the main surface of the inlet baffle plate toward the upper side, the shielding portion is disposed on the outer side in the radial direction than the position where the outer diameter of the inlet of the pipe is projected onto the inlet baffle plate, and the shielding portion has a shielding surface that faces the center position side and suppresses the gas-liquid two phases from scattering toward the outer diameter side of the inlet baffle plate.
Description
Technical Field
The present disclosure relates to a fixed bed reactor.
Background
As a device for reacting a raw material in a facility such as a petrochemical plant facility, a fixed bed reactor is currently used (for example, patent document 1). In such a fixed bed reactor, a reaction layer is disposed at a lower portion, a raw material introduction layer is disposed at an upper portion, and raw materials are supplied from a pipe connected to the upper portion to the inside.
< prior art document >
< patent document >
Patent document 1: japanese patent application laid-open No. 2007-112745
Disclosure of Invention
< problem to be solved by the invention >
A fixed bed reactor of the type described in patent document 1 has the following structure: in the raw material introduction layer, a disk-shaped inlet baffle plate is disposed immediately below an inlet of a pipe leading to a fixed bed reactor, and raw material supplied from above to the inside is received by the inlet baffle plate. For example, depending on the installation conditions of the fixed bed reactor such as the shape and the bending position of the pipe, the raw material may not be uniformly supplied to the entire main surface of the inlet baffle plate. In this case, since the raw material cannot be uniformly diffused in the fixed bed reactor, there is a concern that uneven supply to the reaction layer occurs and the throughput is lowered.
The purpose of the present invention is to provide a fixed bed reactor that can uniformly diffuse a raw material supplied to the inside.
< means for solving the problems >
The present invention includes the following structures.
A fixed bed reactor according to an aspect of an embodiment of the present invention includes: a pipe for introducing a gas-liquid two-phase flow from an upper portion of the fixed bed reactor into an interior; and an inlet baffle plate disposed in the fixed bed reactor so as to face an inlet of the pipe to the fixed bed reactor, wherein the inlet baffle plate is a flat plate disposed horizontally, the inlet of the pipe is disposed directly above a center position of the inlet baffle plate, a shielding portion is provided on a main surface of the inlet baffle plate so as to be directed upward, the shielding portion is disposed on an outer side in a radial direction than a position where an outer diameter of the inlet of the pipe is projected onto the inlet baffle plate, and the shielding portion has a shielding surface directed toward the center position side and is configured to suppress the gas-liquid two phases from scattering toward an outer diameter side of the inlet baffle plate.
The fixed bed reactor according to item [1], wherein the pipe is a curved pipe having a horizontal portion extending in a horizontal direction and a vertical portion bent at a substantially right angle from the horizontal portion and connected to the fixed bed reactor, and the shielding portion is disposed on the opposite side of the horizontal portion from the extending direction.
The fixed bed reactor according to item [2], wherein the shielding surface is disposed so as to face the axis direction of the horizontal portion of the pipe.
The fixed bed reactor according to any one of [1] to [3], wherein the inlet baffle is a polygonal flat plate or a circular plate.
The fixed bed reactor according to any one of [1] to [4], wherein the shape of the shielding surface is a planar shape or a curved shape.
The fixed bed reactor according to any one of [1] to [5], wherein the shielding portion is a plate-like member.
The fixed bed reactor according to item [6], wherein the shielding portion has a flat plate shape, an arc shape, or a cylindrical shape.
The fixed bed reactor according to any one of [1] to [7], wherein when the inclination angle of the shielding surface with respect to the main surface of the inlet baffle is set to 90 degrees when the normal direction of the shielding surface is a horizontal direction, the inclination angle of the shielding surface shifts to 0 degrees when the shielding surface is inclined toward the center side of the inlet baffle, and the inclination angle of the shielding surface shifts to 180 degrees when the shielding surface is inclined toward the outer edge side of the inlet baffle, the inclination angle of the shielding surface is in the range of 40 degrees to 115 degrees.
The fixed bed reactor according to item [8], wherein the shielding surface has an inclination angle in the range of 85 to 110 degrees.
The fixed bed reactor according to [8] or [9], wherein the shielding surface has an inclination angle of 90 degrees.
The fixed bed reactor according to any one of [1] to [7], wherein a normal direction of the shielding surface is a horizontal direction, and an extending direction of the shielding surface is a direction perpendicular to the inlet baffle plate.
< Effect of the invention >
According to the present invention, a fixed bed reactor capable of uniformly diffusing a raw material supplied to the inside can be provided.
Drawings
Fig. 1 is a longitudinal sectional view showing a schematic structure of a fixed bed reactor according to an embodiment.
Fig. 2 is a plan view showing the structure of the raw material introduction layer of the fixed bed reactor according to the embodiment.
FIG. 3 is an enlarged perspective view of the vicinity of the raw material introduction layer of the fixed bed reactor.
Fig. 4 is a schematic view showing the range of the standing direction of the shielding plate.
Fig. 5 is a schematic diagram showing symbols corresponding to respective sizes in a fixed bed reactor.
Fig. 6 is a view showing a first modification of the shielding plate.
Fig. 7 is a diagram showing a second modification of the shielding plate.
Fig. 8 is a graph showing droplet flow distributions of example 1 and comparative example 1.
Fig. 9 is a graph showing a relationship between the inclination angle of the shielding plate and the non-uniformity improvement ratio of the droplet stream.
Fig. 10 is a graph showing droplet flow distributions of example 2 and comparative example 2.
Fig. 11 is a diagram showing the droplet flow distribution of comparative example 3.
Detailed Description
Hereinafter, embodiments will be described with reference to the drawings. For ease of explanation, identical components are given the same reference numerals as much as possible in the drawings, and duplicate explanation is omitted.
In the following description, the x direction, the y direction, and the z direction are directions perpendicular to each other. The x-direction and the y-direction are horizontal directions, and the z-direction is vertical. The x-direction is the axial direction of the horizontal portion 41 of the pipe 4. When the normal line direction of the shielding surface 61 is set to be the horizontal direction, and the inclination angle of the shielding surface 61 with respect to the main surface 51 of the inlet baffle 5 is set to be 90 degrees, the x-direction is the normal line direction of the shielding surface 61 when the inclination angle of the shielding surface 61 is set to be 90 degrees. When the shielding plate 6 is on a flat plate, the y direction is the longitudinal direction of the shielding plate 6. For convenience of explanation, the positive z-direction side is sometimes referred to as the upper side, and the negative z-direction side is sometimes referred to as the lower side.
The schematic structure of the fixed bed reactor 1 according to the embodiment will be described with reference to fig. 1 to 3. Fig. 1 is a longitudinal sectional view showing a schematic structure of a fixed bed reactor 1 according to the embodiment. Fig. 2 is a plan view showing the structure of the fixed bed reactor 1 according to the embodiment in the raw material introduction layer 2. Fig. 3 is a perspective view showing the vicinity of the raw material introduction layer 2 of the fixed bed reactor 1 in an enlarged manner.
Fig. 1 shows an example of a case where the fixed bed reactor is a multitubular fixed bed reactor. In the fixed bed reactor 1, a raw material introduction layer 2 is disposed at the upper part, and a reaction layer 3 is disposed at the lower part. The raw material introduction layer 2 and the reaction layer 3 are separated by a tube sheet surface 7. A pipe 4 for introducing a gas-liquid two-phase flow M (a mixed fluid composed of a gas of a continuous phase and droplets of a dispersed phase) as a raw material into the raw material introduction layer 2 is connected to the upper end of the raw material introduction layer 2. The fixed bed reactor 1 causes the raw material supplied to the raw material introduction layer 2 via the pipe 4 to react with the catalyst in the reaction layer 3, thereby discharging the reaction product from below. In the case of the multitubular fixed bed reactor shown in fig. 1, the reaction layer 3 is constituted by a reaction tube 8 filled with a solid catalyst or the like and a heat medium flow portion provided outside the reaction tube 8 for heating and removing heat from the reaction tube 8. The fixed bed reactor is not limited to the multitubular reactor, and may be a reactor in which all the reaction layers are filled with a solid filler or a solid catalyst.
The pipe 4 is preferably a bent pipe having a horizontal portion 41 extending in the horizontal direction and a vertical portion 42 bent at a substantially right angle from the horizontal portion 41 and connected to the fixed bed reactor 1. As the pipe 4 having such a structure, for example, a single-bend pipe in which two straight pipes are connected by a joint pipe (elbow) bent at 90 degrees is cited. In addition, the pipe 4 may be applied to a pipe of a type other than a single elbow such as a double elbow.
In the present embodiment, in the pipe 4, the horizontal portion 41 is disposed so that the axis thereof becomes the x-direction, and the vertical portion 42 is disposed so that the axis thereof becomes the z-direction. The cross-sectional shape of the pipe 4 is also substantially circular, and the fixed bed reactor 1 is substantially cylindrical with the z-direction as the central axis, and the vertical portion 42 of the pipe 4 is connected to the center of the fixed bed reactor 1 so that the axis coincides with the center position C of the upper substantially circular end face.
With the structure of the pipe 4, as shown in fig. 1, the gas-liquid two-phase flow M passing through the pipe 4 is introduced from above toward below vertically in the center of the fixed bed reactor 1.
An inlet baffle 5 is provided inside the raw material introduction layer 2. The inlet baffle 5 is a flat plate arranged horizontally, and one main surface 51 is arranged vertically upward (in the positive z direction). The inlet baffle 5 is set to a circular plate shape in fig. 1, and is disposed so as to face the inlet 43 of the pipe 4 to the fixed bed reactor 1. More specifically, the inlet 43 of the duct 4 is disposed immediately above the center position C of the inlet baffle 5. The center position C of the circular main surface 51 of the inlet baffle 5 is the same as the center position C of the fixed bed reactor 1. That is, the inlet 43 of the pipe 4, the inlet baffle 5, and the fixed bed reactor 1 are arranged concentrically as shown in fig. 2 in plan view.
In order to prevent the raw material M introduced from the pipe 4 from directly colliding with the reaction layer 3 below to damage the reaction layer 3, the inlet baffle 5 is disposed so as to be interposed between the inlet 43 of the pipe 4 and the reaction layer 3. For buffering purposes, the inlet baffle 5 is generally disposed perpendicularly with respect to the flow of the gas-liquid two-phase stream M. As a result, as shown in fig. 1, the raw material M introduced from the pipe 4 collides with the inlet baffle 5, is reflected, is decelerated, and is supplied to the reaction layer 3.
In the present embodiment in particular, the shielding plate 6 (shielding portion) is erected upward on the main surface 51 of the inlet baffle 5. The shielding plate 6 has a shielding surface 61 facing the center position C side of the inlet baffle 5. As indicated by a in fig. 1, the shielding surface 61 receives a part of the gas-liquid two-phase flow M reflected at the center position C of the inlet baffle 5 and moving radially outward (in the example of fig. 1, the x negative direction side), and reflects it in the opposite direction (in the example of fig. 1, the x positive direction side). This partially suppresses scattering of the gas-liquid two-phase flow M toward the outer diameter side of the inlet baffle 5 by the shielding surface 61.
The fixed bed reactor 1 of the present embodiment can uniformly diffuse the raw material M supplied to the inside by providing the shielding plate 6 so as to block the flow of the gas-liquid two-phase flow M.
The inlet baffle 5 is preferably a polygonal flat plate or a circular plate, and more preferably a circular plate. In the case of a polygonal flat plate, it is preferable to be a regular polygon with a contour close to a circle and a number of vertices, preferably more than ten thousand vertices.
The shielding plate 6 is preferably a flat plate-like member, and the plane of one main surface thereof functions as a shielding surface 61. In this case, the shape of the shielding plate 6 and the shielding surface 61 is rectangular with the y direction as the longitudinal direction.
In the case where the normal direction of the shielding surface 61 is the horizontal direction and the shielding plate 6 is a flat plate, the shielding plate 6 is preferably arranged such that the extending direction of the shielding surface 61 is the direction perpendicular to the inlet baffle 5.
The shielding surface 61 of the shielding plate 6 is preferably disposed so as to face the axis direction (x direction) of the horizontal portion 41 of the duct 4.
As shown in fig. 2, the shielding plate 6 is preferably disposed radially outward of a position where the outer diameter of the inlet 43 of the duct 4 is projected onto the inlet baffle 5.
The fixed bed reactor 1 of the present embodiment can further uniformly diffuse the raw material M supplied to the inside by adopting the structure of the shielding plate 6.
The effect of homogenizing the diffusion of the gas-liquid two-phase flow M by the shielding plate 6 is particularly remarkable in the case where the pipe 4 is a single-turn type as shown in fig. 1 or the like. In the case of the single-bend pipe 4, it is considered that the gas-liquid two-phase flow M flows into the reactor after being bent by 90 degrees in the traveling direction before the inlet of the reactor due to the bend shape, and is strongly influenced by the inertia of the bend due to the bend shape. Therefore, in the conventional reactor, the gas-liquid two-phase flow in the raw material introduction layer 2 is supplied severely unevenly in the region on the side of the horizontal portion 41 of the pipe 4 in the traveling direction, that is, on the opposite side (x negative direction side in the present embodiment) from the horizontal portion 41 across the center position C in a plan view (see fig. 8 a and 10 a). In the present embodiment, the shielding plate 6 can suppress the flow of the gas-liquid two-phase flow M in the direction of the region, and as a result, it is considered that the diffusion of the gas-liquid two-phase flow M can be made uniform. In addition, the gas-liquid two-phase flow M uniformly diffuses in the fixed bed reactor 1 in the outer circumferential direction of the inlet baffle 5, thereby improving the yield of the reaction product.
The shielding plate 6 may be erected obliquely with respect to the inlet baffle 5. Fig. 4 is a schematic view showing the range of the standing direction of the shielding plate 6. As shown in fig. 4, the inclination angle of the shielding surface 61 with respect to the main surface 51 of the inlet baffle 5 is set to 90 degrees when the normal direction of the shielding surface 61 is the horizontal direction. Further, it is defined that the inclination angle of the shielding surface 61 shifts to the 0 degree side when the shielding surface 61 is inclined to the center C side of the inlet baffle 5, whereas the inclination angle of the shielding surface 61 shifts to the 180 degree side when the shielding surface 61 is inclined to the outer edge side of the inlet baffle 5. When the shielding plate 6 is flat, the extending direction of the shielding surface 61 is perpendicular to the inlet baffle 5. In this case, as shown in the angle range R1 of fig. 4, the inclination angle of the shielding surface 61 is preferably in the range of 40 degrees to 115 degrees. As shown in the angle range R2 of fig. 4, the inclination angle of the shielding surface 61 is more preferably in the range of 85 degrees to 110 degrees. Further, the inclination angle of the shielding surface 61 is more preferably 90 degrees.
By setting the inclination angle of the shielding surface 61 as described above, the raw material M supplied to the inside of the fixed bed reactor 1 can be further uniformly diffused.
Fig. 5 is a schematic diagram showing symbols corresponding to respective sizes in the fixed bed reactor 1. Fig. 5 (a) is a longitudinal sectional view similar to fig. 1, and fig. 5 (B) is a plan view similar to fig. 2.
As shown in fig. 5 (a) and (B), the pipe diameter is D, and the reactor diameter is D. As shown in fig. 5 (a), the vertical coordinate of the inlet baffle 5 with respect to the tube sheet 7 is set to H, the height of the joint between the tube sheet 7 and the tube 4 and the reactor 1 is set to H, and the z-direction height of the shielding plate 6 is set to E. As shown in fig. 5 (B), the distance from the center position C of the inlet baffle 5 to the shielding plate 6 is L, the diameter of the inlet baffle 5 is F, and the width of the shielding plate 6 in the longitudinal direction (y-direction) is G.
The diameter F of the inlet baffle 5 is preferably 0.3D or more and 0.4D or less. The installation position H/H (0.ltoreq.h/H.ltoreq.1) of the inlet baffle 5 is preferably 0.2 to 0.8. The distance L of the shielding plate 6 from the center position C is preferably larger than the duct diameter d. The width G of the shielding plate 6 is preferably larger than the duct diameter d. The height E of the shielding plate 6 is preferably 0.2H or more and is not in contact with the upper wall surface of the reactor 1.
In the present embodiment, the flow velocity of the gas-liquid two-phase flow M of the raw material through the pipe 4 is preferably 8 to 15M/s. In addition, the volume fraction of the droplet concentration of the gas-liquid two-phase flow M is preferably less than 10%.
By applying the conditions of these various parameters, the raw material M supplied to the inside of the fixed bed reactor 1 can be further uniformly diffused.
Fig. 6 is a diagram showing a first modification of the shielding plate 6A. As shown in fig. 6, the shielding plate 6A may be arc-shaped. The arc shape of the shielding plate 6A is formed centering on the center position C of the inlet baffle 5. In this case, the shielding surface 61A has a curved surface shape along an arc shape.
In the arc-shaped shielding plate 6A of the first modification, when the diameter F of the inlet baffle 5 is smaller than ∈2d, that is, when the shielding plate is flat, the plate width G of the duct diameter d cannot be obtained, and it is effective to satisfy the condition that the width H of the shielding plate 6A in the longitudinal direction is larger than the duct diameter d. The width J of the shielding plate 6A is preferably pi d/2 or more and less than pi d/. Cndot.2. When the arc-shaped shielding plate 6A is inclined and erected, the shielding surface 61A is preferably inclined as well.
Fig. 7 is a diagram showing a second modification of the shielding plate 6B. As shown in fig. 7, the shielding plate 6B may be cylindrical. The cylindrical shape of the shielding plate 6B is formed centering on the center position C of the inlet baffle 5. In this case, the shielding surface 61B is a cylindrical inner peripheral surface, and is curved. The inner diameter of the cylindrical shape of the shielding plate 6B is preferably larger than the pipe diameter d. When the cylindrical shielding plate 6B is inclined and erected, the shielding surface 61B is preferably inclined as well.
The fixed bed reactor used in the present embodiment may be of a single tube type or a multitubular type. In the case of a single-tube reactor, the outer diameter and length of the reactor are not limited, and are arbitrarily determined from the viewpoints of securing the quality speed, diffusing the material into the reactor, and the like. In a fixed bed flow-through reaction in which a reaction raw material is continuously brought into contact with a heterogeneous solid catalyst, a multitubular reactor is generally used when the reaction is accompanied by heat generation or heat absorption. In the case of a multitube reactor, a cylindrical straight tube having the same outer diameter, wall thickness and length is usually used as the reaction tube, and the inner diameter of the reaction tube is preferably determined so as to be 4 times or more the diameter of the packed catalyst, but the reaction tube is not particularly limited thereto, although the reaction tube is industrially selected in the range of about 15 to 50 mm.
The reaction that can be applied to the fixed bed reactor of the present embodiment is not particularly limited. In general, the reaction carried out in a fixed bed reactor is sufficient, and examples thereof include production of ethylene oxide by oxidation of ethylene, production of acrolein and acrylic acid by oxidation of propylene, production of methacrolein and methacrylic acid by oxidation of iso-ethylene, production of anhydrous maleic acid by oxidation of benzene, production of aziridine by dehydration of monoethanolamine, production of N-vinyl resin-2-pyrrolidone by dehydration of N- (2-hydroxyethyl) -2-pyrrolidone, production of acrylonitrile by ammoxidation of propylene, production of ethyl acetate by direct addition of acetic acid to ethylene, production of vinyl acetate by oxidative acetoxylation of propylene, production of propylene acetate by oxidative acetoxylation of propylene, production of ethylene by hydrogenation of acetylene, production of cyclohexane by hydrogenation of benzene, production of styrene monomer by hydrogenation of propane, production of propylene by dehydrogenation of 1-butene isomerization, production of 2-butene by isomerization of propylene oxide, production of ethanol by hydration of propylene, production of 2-propanol by hydration of propylene, and the like. Further, the method is preferably applied to a reaction of a type in which a gas-liquid two-phase flow is introduced into a reactor, and specific examples thereof include production of vinyl acetate by oxidative acetoxylation of ethylene, production of allyl acetate by oxidative acetoxylation of propylene, and the like.
[ example ]
In order to confirm the effectiveness of the above embodiment, a calculation simulation was performed. The main calculation conditions are as follows.
Using software: universal numerical fluid analysis software ANSYS (registered trademark) Fluent (registered trademark) manufactured by ANSYS corporation
Continuous phase (gas=gas phase) governing equation: N-S equation, continuous
Turbulence model: k-epsilon model
Gas-liquid two-phase flow analysis: euler-Lagrange type (analysis of gaseous fluid by Euler type and liquid droplets by Lagrange type)
Dispersed phase flow: liquid phase
Particle tracking method (DPM (DiscretePhaseModel)): oneWayCouping
Analysis symmetry: pipeline and reactor
(1) Example 1
The ratio of the pipe diameter D, the diameter of the circular-shaped bottom plate (the diameter F of the inlet baffle 5), and the reactor diameter D was set to 1:5:20. the position H/H of the inlet baffle 5 is set to 0.4. The shape of the shielding plate 6 was set to be a flat plate, the height E was set to 0.2H, and the width G was set to 0.2D. The flow rate of the gas-liquid two-phase flow M was set to 10M/s, and the droplet concentration was set to 5% by mass. Under these conditions, the droplet flow distribution of the raw material introduction layer 2 of the fixed bed reactor 1 in plan view was measured. The droplet stream is the product of the droplet concentration and the vertical gas flow rate (droplet concentration x gas flow rate).
(2) Comparative example 1
The same conditions as in example 1 were set except that the shielding plate 6 was not provided.
Fig. 8 is a diagram showing droplet flow distribution in a plane including the main surface 51 of the inlet baffle 5 of example 1 and comparative example 1. Fig. 8 (a) shows the result of comparative example 1, and (B) shows the result of example 1. In fig. 8, the distribution is illustrated in such a manner that the smaller the droplet stream is, the closer to white, and the larger the droplet stream is, the closer to black.
As shown in fig. 8 a, in the state where the shielding plate 6 is not present, the droplet flow is deviated to the left side (the region opposite to the horizontal portion 41 of the pipe 4) in the drawing, and the standard deviation of the droplet flow in the entire plane is 3.7x10 -5 It is known that unevenness occurs in the droplet flow as a whole plane. On the other hand, as shown in fig. 8 (B), in the state where the shielding plate 6 is present, it is found that the portion having a thicker color than (a) is reduced, and the unevenness of the whole is suppressed. The standard deviation of the droplet stream over the entire plane was 1.3X10 -5 Can be reduced to about 1/3 as compared with (A) in which the shielding plate 6 is not present.
As described above, according to the results of example 1 and comparative example 1 shown in fig. 8, it is shown that by providing the shielding plate 6 in the inlet baffle 5, the droplet flow distribution in the plan view of the raw material introduction layer 2 of the fixed bed reactor 1 can be made uniform, and the gas-liquid two-phase flow M of the raw material supplied to the inside can be uniformly dispersed.
(3) Inclination angle of shielding plate
The same conditions as in example 1 were set except that the inclination angle of the shielding plate 6 was further changed. Under the conditions described with reference to fig. 4, the inclination angles of the shielding plate 6 are set to 15 degrees, 30 degrees, 45 degrees, 75 degrees, 90 degrees, 110 degrees, and 120 degrees. At each inclination angle, the droplet stream distribution was measured by performing the same simulation as in example 1, and the standard deviation of the droplet stream was calculated. The standard deviation of comparative example 1 without the shielding plate 6 was set as a reference (base), and the reduction rate of the standard deviation of each tilt angle was calculated as the improvement rate (base improvement rate) of the unevenness of the droplet stream with respect to the comparative example.
Fig. 9 is a diagram showing a relationship between the inclination angle of the shielding plate 6 and the non-uniformity improvement ratio of the droplet stream. The horizontal axis of fig. 9 shows the inclination angle (°) of the shielding plate 6. The vertical axis of fig. 9 shows the improvement rate to the base.
As shown in fig. 9, the improvement ratio was 50% or more in the range of the inclination angle of 40 degrees to 115 degrees, and it was found that the effect of sufficiently improving the unevenness of the droplet flow was produced. In addition, in the range of the inclination angle of 85 degrees to 110 degrees, the improvement rate was 60% or more, and it was found that the effect of improving the unevenness of the droplet flow was further generated. Further, when the inclination angle was 90 degrees, the improvement rate was the largest, and it was found that the effect of improving the unevenness of the droplet flow was the best.
As described above, the simulation result shown in fig. 9 shows that the inclination angle of the shielding plate 6 (shielding surface 61) is preferably in the range of 40 degrees to 115 degrees, more preferably in the range of 85 degrees to 110 degrees, and even more preferably in the range of 90 degrees.
(4) Example 2
Except that the ratio of the pipe diameter D, the diameter of the circular-shaped bottom plate (the diameter F of the inlet baffle 5), and the reactor diameter D was set to 3:4:10, the same conditions as in example 1 were set except that the shape of the shielding plate 6A was set to be circular arc, and the droplet flow distribution in plan view of the raw material introduction layer 2 of the fixed bed reactor 1 was measured in the same manner as in example 1. The width J of the shielding plate 6A is set to 0.42D.
(5) Comparative example 2
The same conditions as in example 2 were set except that the shielding plate 6A was not provided.
Fig. 10 is a diagram showing droplet flow distribution in a plane including the main surface 51 of the inlet baffle 5 of example 2 and comparative example 2. Fig. 10 (a) shows the result of comparative example 2, and (B) shows the result of example 2. The flow velocity distribution of fig. 10 is shown in the same manner as fig. 8.
In the state where the shielding plate 6A is not present as shown in fig. 10 (a), the droplet flow is deviated to the left side (the region opposite to the horizontal portion 41 of the pipe 4) in the drawing, and the standard deviation of the droplet flow in the entire plane is 9.7x10 -3 It is known that unevenness is generated in the droplet stream as a whole plane. On the other hand, in the state where the shielding plate 6A is present as shown in fig. 10 (B), it is found that the portion having a thicker color than (a) is reduced, and the unevenness of the whole is suppressed. The standard deviation of the droplet stream over the entire plane was 2.0X10 -3 Can be reduced to about 1/5 as compared with (A) in which the shielding plate 6 is not present.
As described above, according to the results of example 2 and comparative example 2 shown in fig. 10, it is shown that even by providing the arc-shaped shielding plate 6A on the inlet baffle 5, the droplet flow distribution in the plan view of the raw material introduction layer 2 of the fixed bed reactor 1 can be made uniform, and the gas-liquid two-phase flow M of the raw material supplied to the inside can be uniformly dispersed.
(6) Comparative example 3
The same conditions as in example 2 were set except that the shielding plate 6A was disposed inside the duct diameter d. The width J of the shielding plate 6A is set to 0.27D.
Fig. 11 is a diagram showing droplet flow distribution in a plane including the main surface 51 of the inlet baffle 5 of comparative example 3. The flow velocity distribution in fig. 11 is shown in the same manner as in fig. 8 and 10. According to the result of comparative example 3 shown in FIG. 11, if the shielding plate 6A is positioned inside the duct 4, the standard deviation of the droplet stream is 5.0X10 -3 Although the liquid droplet distribution can be reduced to about 1/2 as compared with comparative example 2, the deviation of the liquid droplet distribution is shown in the same manner as in the case of the non-shielding plate 6A of comparative example 2. Therefore, as shown in fig. 2, 6, and 7, it is preferable that the shielding plates 6, 6A, and 6B are arranged outside the position where the outer diameter of the inlet 43 of the duct 4 is projected on the inlet baffle 5 in the radial direction.
The present embodiment has been described above with reference to specific examples. However, the present invention is not limited to these specific examples. The invention of which one skilled in the art can add appropriate design changes to these specific examples is included in the scope of the present invention as long as the invention includes the features of the present invention. The elements, arrangement, conditions, shape, and the like included in each specific example are not limited to examples, and may be appropriately changed. The elements included in the specific examples described above can be appropriately combined without technical contradiction.
In the above-described embodiment, the shielding plate 6 of the plate-like member is provided on the inlet baffle 5, but the shielding plate may be other than the plate-like member as long as the shielding plate has the shielding surface 61 for suppressing the gas-liquid two-phase flow M from scattering to the outer diameter side of the inlet baffle 5. For example, a block-shaped shielding portion such as a rectangular parallelepiped or a cube may be provided on the main surface 51 of the inlet baffle 5 instead of the shielding plate 6, and the block-shaped shielding portion may have a shielding surface 61.
The international application is based on japanese patent application No. 2020-211664 filed on 12/21 in 2020, and the entire contents of No. 2020-211664 are cited in the international application.
Symbol description
1 fixed bed reactor
4 pipeline
41 horizontal part
42 vertical portion
5 inlet baffle
6. 6A, 6B shielding plate (shielding part)
7 tube plate surface
8 reaction tube
61. 61A, 61B.
Claims (11)
1. A fixed bed reactor comprising:
a pipe for introducing a gas-liquid two-phase flow from the upper part of the fixed bed reactor into the interior; and
an inlet baffle plate which is arranged in the fixed bed reactor opposite to an inlet of the pipeline which leads to the fixed bed reactor,
the inlet baffle is a flat plate arranged horizontally,
the inlet of the duct is disposed directly above the center of the inlet baffle,
the inlet baffle plate has a main surface, and a shielding portion is provided on the main surface of the inlet baffle plate so as to be upward and vertically disposed on the outer side in the radial direction than a position where the outer diameter of the inlet of the pipe is projected onto the inlet baffle plate, the shielding portion having a shielding surface that faces the center position side and suppresses the gas-liquid two phases from scattering toward the outer diameter side of the inlet baffle plate.
2. The fixed bed reactor according to claim 1, wherein,
the pipe is a bent pipe having a horizontal portion extending in a horizontal direction and a vertical portion bent at a substantially right angle from the horizontal portion and connected to the fixed bed reactor,
the shielding portion is disposed on the opposite side of the extending direction of the horizontal portion.
3. The fixed bed reactor according to claim 2, wherein,
the shielding surface is disposed so as to face the axis direction of the horizontal portion of the duct.
4. A fixed bed reactor according to any one of claim 1 to 3, wherein,
the inlet baffle is a polygonal flat plate or circular plate.
5. The fixed bed reactor according to any one of claims 1 to 4, wherein,
the shape of the shielding surface is a plane shape or a curved surface shape.
6. The fixed bed reactor according to any one of claims 1 to 5, wherein,
the shielding part is a plate-shaped member.
7. The fixed bed reactor according to claim 6, wherein,
the shielding part is in a shape of a flat plate, an arc or a cylinder.
8. The fixed bed reactor according to any one of claims 1 to 7, wherein,
in the case where the inclination angle of the shielding surface with respect to the main surface of the inlet baffle is set to 90 degrees when the normal direction of the shielding surface is set to the horizontal direction, the inclination angle of the shielding surface shifts to 0 degrees when the shielding surface is inclined toward the center side of the inlet baffle, and the inclination angle of the shielding surface shifts to 180 degrees when the shielding surface is inclined toward the outer edge side of the inlet baffle,
the inclination angle of the shielding surface is in the range of 40-115 degrees.
9. The fixed bed reactor according to claim 8, wherein,
the inclination angle of the shielding surface is in the range of 85-110 degrees.
10. A fixed bed reactor according to claim 8 or 9, wherein,
the inclination angle of the shielding surface is 90 degrees.
11. The fixed bed reactor according to any one of claims 1 to 7, wherein,
the normal direction of the shielding surface is the horizontal direction,
the extending direction of the shielding surface is a direction perpendicular to the inlet baffle plate.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2020211664 | 2020-12-21 | ||
| JP2020-211664 | 2020-12-21 | ||
| PCT/JP2021/045840 WO2022138286A1 (en) | 2020-12-21 | 2021-12-13 | Fixed-bed reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116648304A true CN116648304A (en) | 2023-08-25 |
Family
ID=82157925
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202180086162.XA Pending CN116648304A (en) | 2020-12-21 | 2021-12-13 | fixed bed reactor |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JPWO2022138286A1 (en) |
| CN (1) | CN116648304A (en) |
| TW (1) | TWI800160B (en) |
| WO (1) | WO2022138286A1 (en) |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0463126A (en) * | 1990-07-02 | 1992-02-28 | Uop Inc | Fluid distribution device |
| US5160513A (en) * | 1991-11-13 | 1992-11-03 | Uop | Inlet stream debris collection method and apparatus |
| RU2284217C2 (en) * | 2001-03-01 | 2006-09-27 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Reactor |
| EP2918332A1 (en) * | 2014-03-14 | 2015-09-16 | Morten Müller Ltd., ApS | Scale collection and predistribution tray for vessel with downwards two-phase flow |
| KR101989328B1 (en) * | 2016-11-25 | 2019-06-14 | 차이나 페트로리움 앤드 케미컬 코포레이션 | Impact-Reducing Uniform-Flowing Disc and Reactor |
-
2021
- 2021-12-13 WO PCT/JP2021/045840 patent/WO2022138286A1/en active Application Filing
- 2021-12-13 JP JP2022572172A patent/JPWO2022138286A1/ja active Pending
- 2021-12-13 CN CN202180086162.XA patent/CN116648304A/en active Pending
- 2021-12-15 TW TW110146979A patent/TWI800160B/en active
Also Published As
| Publication number | Publication date |
|---|---|
| WO2022138286A1 (en) | 2022-06-30 |
| JPWO2022138286A1 (en) | 2022-06-30 |
| TW202235150A (en) | 2022-09-16 |
| TWI800160B (en) | 2023-04-21 |
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