Reactor loading for efficient flow distribution

Abstract

summary This disclosure relates to a reactor having an inlet above an outlet, and includes a catalyst bed having a plurality of material layers in the following order from the inlet to the outlet: a first layer providing flow resistance corresponding to a pressure loss dpm1 per meter, a second layer providing flow resistance corresponding to a pressure loss dpm2 per meter, Here, The combined height of the first and second layers is at least 4 m, the height of the second layer is at least 0.5 m, the pressure loss per meter of the second layer dpm2 is at least 20% greater than the pressure loss per meter of the first layer dpm1, and the first layer, the second layer, and any further layers are supported by a single catalyst support. This offers the associated advantage of providing active redistribution of liquid flow without requiring an internal structure, except for a single catalyst support beneath multiple catalyst layers.

Description

Technical Field

[0001] The present disclosure relates to the field of chemical engineering, and more particularly to the efficient management of flows in large fixed-bed reactors such as trickle-bed reactors.

Background Art

[0002] Background Art In order to maximize the utilization of the reactor volume in a catalytic reactor, especially in a large reactor, an efficient distribution of reactants and thermal energy is required.

[0003] Normally, mechanical devices such as loading distributors are installed to redistribute the feed, products, and energy, but such devices are expensive and occupy space in the reactor.

[0004] Summary of the Invention To enable an efficient distribution of reactants and an efficient utilization of the reactor volume, we propose loading the catalytic active material so as to create a local resistance to the flow, i.e., a pressure loss, which increases the radial distribution of the flow. This resistance to the flow is provided, for example, by providing a reactor zone with low flow resistance by making the catalyst particles small. When the flow enters a region of high resistance, the radial diffusion increases and the flow is redistributed, thus reducing the radial variations in composition and temperature.

[0005] Technical Problem In a chemical reaction, the availability of reactants, temperature, and thermal energy determine the degree of progress of the reaction.

[0006] In many industrial applications, some or all of the reactants are typically in the liquid phase, and an appropriate catalyst is required to promote the desired chemical reaction. To ensure that the reactants contact the catalyst efficiently and uniformly, a liquid distributor is often used to distribute the reactants uniformly throughout the catalyst bed.

[0007] A typical reactor design is a vertical cylindrical reactor loaded with catalyst particles, where liquids and gases react. Typically, liquid reactants flow in from the top and out from the bottom, while gaseous reactants flow either in the same direction or in the opposite direction. Theoretically, random loading of numerous fine particles ensures uniform distribution; however, in practice, inflow and loading characteristics can lead to regions of high reaction activity or blockages. Under localized conditions, solid deposits can adhere to the catalyst surface, further increasing reaction heterogeneity by obstructing flow.

[0008] To minimize such distribution non-uniformity, it is common practice to redistribute the flowing gas and liquid at regular intervals, for example, by providing one or more mechanical redistribution trays along the cylindrical axis of the reactor. However, such trays occupy reactor volume and reduce the reactor's conversion capacity, so it is desirable to perform redistribution without sacrificing reactor volume.

[0009] The evaluation of redistribution is usually performed by assessing the temperature gradient within the reactor, because temperature measurement is inexpensive and provides a fast response, and in exothermic reactions, temperature measurement also reflects both distribution heterogeneity and reactivity heterogeneity.

[0010] U.S. Patent No. 3,732,078 discloses the redistribution of reactor flow using a deflector followed by large solid particles, and evaluates its effect by assessing the bulk catalyst performance.

[0011] U.S. Patent No. 9,732,774 employs a similar approach, showing that the reactor consists of a processing zone and a redistribution zone, with the processing zone being composed of a highly porous material, the effect of which is tested by the distribution of water flow within the reactor. [Prior art documents] [Patent Documents]

[0012] [Patent Document 1] U.S. Patent No. 3732078 [Patent Document 2] U.S. Patent No. 9732774 [Overview of the project] [Problems that the invention aims to solve]

[0013] Evaluations of redistribution methods using open redistribution zones installed in operating reactors have shown that temperature fluctuations throughout the reactor are inappropriately large, and methods that achieve lower radial temperature fluctuations are desired.

[0014] definition In the following, a cylindrical catalytic reactor is interpreted as a mechanical unit comprising a substantially cylindrical central portion having a substantially vertical axis, at least one inlet position and one outlet position, and containing a certain amount of catalyst particles and any mechanical and non-catalytic particles. The substantially cylindrical portion may be configured to have upper and lower ends where the inlet and outlet can be located. The ends are dome-shaped, and the reactor is typically designed to withstand high pressures up to several MPa. The reactor may have additional inlets and outlets located on the periphery of the cylinder. The size of the reactor is typically 3m to 5m in diameter and 10m to 40m or more in height.

[0015] A reactor can receive a single-phase liquid or gas flow, or it can receive or produce a two-phase liquid-gas flow.

[0016] When the reactor flow is two-phase, the reactor is of a type called a trickle bed reactor, in which the liquid and gas flow in the same direction.

[0017] Multiple sensors, particularly temperature sensors, can be placed inside the reactor. The radial temperature span refers to the maximum temperature difference between sensors placed at substantially the same vertical (axial) position. The axial temperature span between different vertical positions is usually calculated from the difference between two average values ​​measured at similar vertical positions.

[0018] The present invention mainly relates to redistribution in the bulk catalyst region. A bulk catalyst is defined as a catalyst in which macropores with a diameter exceeding 100 nm occupy less than 50% of the pore volume in measurements by the mercury penetration method.

[0019] The flow in a cylindrical reactor is generally driven by an axial propulsion component and a radial diffusion component. The axial propulsion flow refers to the flow driven by a propulsion force that flows from the inlet to the outlet along the cylindrical axis of the reactor. The radial diffusion flow refers to the flow that is driven by diffusion and the deflection of the axial propulsion flow and is substantially orthogonal to the axial propulsion flow.

Means for Solving the Problem

[0020] Solutions to the Problem Typical trickle bed reactors in which liquid oil usually reacts with gaseous hydrogen in the presence of a solid catalyst, such as hydrotreating reactors and hydrocracking reactors, can have a diameter of 3 to 5 m and a height of 40 m, although smaller or larger dimensions also exist. For efficient operation, the catalyst material is loaded into individual beds, and mechanical internals promote mixing between the beds and gas / liquid contact.

[0021] As described above, phase separation due to axial flow occurs in the beds of large reactors, which may cause poor distribution in the lower layer. Although this problem is solved by a design method that keeps the height of the long bed low, practical constraints such as the modification of existing plants may sometimes require deviation from this method.

[0022] To minimize the impact of such a large reactor bed, fluid redistribution is desirable. The method of providing open channels to guide the flow path and distribute the flow is attractive, but to find a practical solution, it is necessary to consider the theory of the flow mode of the trickle bed, and the distribution effect by the open channels remains minimal. Transport in a cylindrical trickle bed reactor is axial convection (from top to bottom) driven by the inlet pressure and gravity, and radial diffusion from the center towards the outer periphery of the reactor. At typical Reynolds numbers (>10) in a hydrotreating or hydrocracking reactor, the Peclet number (Pe) related to the transport from axial advection to radial diffusion is close to 12 (about 12) for both gas and liquid.

[0023] To calculate the ratio of the bed height (L) to the bed diameter (Ld), the ratio of the two values is obtained from the relationship of the Peclet number:

Equation

[0024] Therefore, a redistribution zone height of 3 × 1.73 = 5.2 m is required for a redistribution zone that achieves complete redistribution across a 3 m diameter bed. The particle shape and orientation may slightly change this ratio and the required zone height, but do not significantly affect the redistribution effect. <00,00105>

[0025] On the other hand, when using a material with a large pressure loss, the force due to the increased pressure loss increases the radial diffusion transport and decreases the Peclet number, so the required zone height for complete redistribution across a 3 m diameter bed can be reduced. Furthermore, by using such a low void material, the catalytic active volume in the reactor does not decrease. It may even be possible to achieve this without an increase in the pressure loss across the entire bed if the top layer of the bed has a void slightly higher than the desired value and the lower layer has a low void.

[0026] The technique of placing a low-pressure-loss catalyst layer above a higher-pressure-loss catalyst layer is known as a hold-down top layer on a catalyst material, and aims to redistribute coarse particles and prevent fine catalyst particles from floating up. The hold-down layer performs a purely mechanical function and is usually composed of inert balls. Furthermore, in grading at the inlet of a catalytic reactor, larger particles can generally be loaded on top of smaller particles. The purpose of this grading is to capture impurities in the feed containing metals in organometallic compounds. Therefore, such grading catalysts are designed to have a certain catalytic activity and to capture solid materials while minimizing the impact on the process. Grading catalysts are porous materials, with large pores dominant in which metals can be deposited. Furthermore, the large particle size allows for the deposition of impurities between particles without obstructing the flow. Typical pore sizes for this type of grading material are such that at least 50% of the pore volume, as measured by mercury pore spectroscopy, is greater than 100 nm in diameter. Typical particle sizes for grading catalysts are greater than 5 mm (3 / 16 inch). The loading of a classification catalyst is typically characterized by one or more of the following: a catalyst with a significant pore volume in large pores, for example, 50% of the pore volume in pores with a radius greater than 500 Å; multiple small catalyst layers, each less than 2000 mm in size; and catalytically active materials having different activities, such as metal content differing by more than 20% between adjacent layers. Such loading of classification catalysts is not considered part of this specification.

[0027] The present invention relates to bulk catalysts for processes smaller than classification, such as 5 mm or 3 mm. Furthermore, bulk catalysts typically exhibit minimal variation in activity and composition (e.g., metal content) (less than 50%, less than 20%, or substantially identical). Since the present invention relates particularly to hydrocracking processes where there is a risk of thermal runaway in the event of a distribution failure, the catalyst may include zeolite or other materials active in hydrocracking.

[0028] A practical consideration when examining catalysts of different sizes is activity. In many processes, smaller catalyst particles increase practical activity because the transport of reactants within the catalyst is not a limiting factor. Therefore, using larger particles may slightly reduce overall activity. However, if the effects of the present invention are obtained by using layers of material that are moderately larger than normally applied and layers of material that are moderately smaller than normally applied, the activity reduction of the first layer is compensated for by the second layer, and as a result, the total activity and pressure loss are maintained as in the case of a conventionally designed catalyst load.

[0029] Advantageous effects of the invention A first aspect of this disclosure relates to a reactor in which the inlet is located above the outlet, the reactor includes a catalyst bed comprising a plurality of material layers in the following order from the inlet to the outlet: a first layer providing flow resistance corresponding to a pressure loss dpm1 per meter, a second layer providing flow resistance corresponding to a pressure loss dpm2 per meter, The combined height of the first and second layers is at least 4 m, the height of the second layer is at least 0.5 m, the pressure loss per meter of the second layer dpm2 is at least 20% greater than the pressure loss per meter of the first layer dpm1, and the first layer, the second layer, and any further layers are supported by a single catalyst support.

[0030] This provides the advantage of providing active redistribution of the liquid flow without requiring internal structure, except in cases where there is a single catalyst support beneath multiple catalyst layers. The presented first and second layers do not preclude the presence of additional layers above, between, or below the first and second layers in the catalyst bed, and additional catalyst beds and internal structures may exist within the reactor.

[0031] In a second embodiment of this disclosure, with respect to the reactor of the first embodiment, The material further comprises a third layer of porous material positioned below the second layer and providing flow resistance equivalent to a pressure loss per meter dpm3, wherein the material of the third layer comprises a porous heat-resistant support and a catalytically active metal, wherein the pressure loss per meter of the second layer is at least 20% greater than the pressure loss per meter provided by the third layer.

[0032] This provides the associated benefit of providing an intermediate layer for redistribution between two layers with low total pressure loss.

[0033] A third embodiment of the present disclosure relates to a reactor of a prior embodiment, wherein the material of the first layer, the material of the second layer, or, if present, the material of the third layer, for example, several or all of the materials of these layers, includes a porous heat-resistant support and a catalytically active metal.

[0034] This results in the associated advantage of redistribution occurring by the material supporting the catalytic reaction.

[0035] A fourth embodiment of the present disclosure relates to the reactor of the preceding embodiment, wherein the shape of the reactor is substantially a vertical cylinder and the ratio of the height to the diameter of the first layer is less than 4:1.

[0036] This, in turn, provides the benefit of ensuring sufficient distribution in Zone 1.

[0037] A fifth embodiment of the present disclosure relates to a reactor described in the claims of a prior embodiment, wherein the shape of the reactor is substantially vertically cylindrical, and the ratio of the total height to diameter of the first layer, the second layer, and the third layer of porous material, if present, is greater than 4:1, for example 5:1 or 6:1.

[0038] This offers the related advantage of enabling efficient redistribution within the reactor bed, exceeding the limitations of conventional designs.

[0039] A sixth embodiment of this disclosure relates to the reactor of the aforementioned embodiment, The reactor is substantially vertically cylindrical in shape, where the ratio of the total height to diameter of the first layer, the second layer, and, if present, the third layer of porous material is less than 10:1, for example, 8:1 or 7:1.

[0040] This has the associated advantage of enabling efficient redistribution within a high reactor bed, within practical size constraints.

[0041] A seventh embodiment of the present disclosure relates to a reactor of a prior embodiment, wherein at least 50% of the porous material of at least one of the first layer, the second layer, and the third layer, if present, has an average dimension along the shortest axis of 0.1 mm to 0.5 mm, or 1 mm to 3 mm, or ~5 mm, and the ratio of the average dimension in the longest axis direction to the average dimension in the shortest axis direction is 1:1 to 20:1.

[0042] This provides the associated advantage that the porous material is suitable as a catalyst. Alternative ratios can be at least 1.5:1 or 2:1. It is also possible to use ratios below the upper limits of 5:1, 10:1, or 15:1.

[0043] An eighth embodiment of the present disclosure relates to a reactor of a prior embodiment and is characterized in that at least 50% of the porous material of the first layer, the second layer and, if present, the third layer, for example, multiple or all of these layers, has a tetrahedron, trihedron, annular or cylindrical shape.

[0044] This provides the related advantage that the porous material is suitable as a catalyst with good local distribution of gas, liquid, reactants, and products.

[0045] A ninth embodiment of the present disclosure relates to a reactor of a prior embodiment, wherein at least 50% of the porous material of the first layer, the second layer and, if present, the third layer, for example, multiple or all of these layers, is an extruded material.

[0046] This comes with the associated advantage that such extruded materials can be manufactured in a cost-effective manner.

[0047] A tenth embodiment of the present disclosure relates to a reactor of a prior embodiment, wherein the weight concentrations of each catalytically active metal in the materials of Zone 1 and Zone 2, or Zone 3, if present, differ by less than 20% of the total weight concentration of catalytically active metals, but the zones differ in size or shape.

[0048] This results in the reactor bed having the associated advantage of maintaining efficient distribution while supporting a single catalytic function.

[0049] An eleventh embodiment of the present disclosure relates to a reactor of a prior embodiment, wherein the catalytically active metal of the Zone 1 material and the Zone 2 material, or the Zone 3 material if present, is active in hydrocracking, and optionally includes zeolite or molecular sieve.

[0050] Since the present invention relates particularly to a hydrocracking process that carries a risk of thermal runaway in the event of a distribution failure, the catalyst may include a zeolite or other material that is active in hydrocracking.

[0051] Further aspects of the present disclosure relate to a method for fluid redistribution in a fixed-bed reactor having a liquid inlet above a liquid outlet, comprising the step of providing a first material layer positioned on top of a second material layer in a single-bed support with a single catalyst support, wherein the combined height of the first and second material layers is at least 4 m, the height of the second layer is at least 0.5 m, and the pressure loss per meter in the second material layer is at least 20% higher than the pressure loss per meter in the first material layer.

[0052] This provides the associated advantage of providing active redistribution of liquid flow without requiring an internal structure, except in cases where there is a single catalyst support beneath multiple catalyst layers. [Brief explanation of the drawing]

[0053] [Figure 1] Figure 1 shows an example of catalyst loading in a reactor according to the present invention. [Figure 2] Figure 2 shows an example of catalyst loading in a reactor according to the present invention. [Figure 3] Figure 3 shows an example of catalyst loading in a reactor using conventional technology. [Figure 4] Figure 4 shows the thermal performance of the two beds in the reactor according to the present invention. [Modes for carrying out the invention]

[0054] Figure 1 Figure 1 shows an example of catalyst loading in the lower part of a reactor according to the present invention. The top of the column is a void, followed below by an inert material layer (A) to fix the lower layers and ensure initial distribution. The total height of A is 300 mm. Below this layer are two layers of activated hydrocracking catalysts B1 and B2. B1 is a 1 / 8-inch trilobed extruded body with a length of 5500 mm and an estimated pressure drop of 0.08 bar / m. B2 is a 1 / 16-inch cylindrical extruded body with a length of 5500 mm and an estimated pressure drop of 0.15 bar / m. To hold the 150 mm extruded body layer C, inert ceramic balls are placed on the catalyst support that holds all layers (A, B1, B2, C) and are located above the quenching section that receives cooling hydrogen (including the bubble cap mixing zone and void zone, totaling 370 mm here, typically less than 500 mm). Below the mixing zone, two inert layers totaling 300 mm are further arranged: an inert tablet-shaped material layer to fix the lower layers and ensure initial distribution, and another inert material layer to further distribute the flow and capture impurities. Below these layers, two more layers of active hydrogenolysis catalysts F1 and F2 are placed. F1 is a 5500 mm 1 / 8-inch tri-lobed extruded body with an estimated pressure drop of 0.12 bar / m, and F2 is a 5500 mm 1 / 12-inch quad-lobed extruded body with an estimated pressure drop of 0.18 bar / m. Subsequently, a 1350 mm layer (G) of hydrogenation finishing catalyst (1 / 20-inch tri-lobed) is placed, and before the hold-down layer H, three different sizes of inert ceramic balls 1200 mm arranged on a catalyst support are placed.

[0055] Figure 2 Figure 2 shows an example of catalyst loading into the lower part of a reactor according to the present invention. The top of the tower is a void, followed below by an inert material layer (A) to fix the lower layer and ensure initial distribution. The total height of A is 300 mm. Below this layer are three layers of activated hydrogenolysis catalysts B1, B2, and B3. B1 is a 1 / 8-inch trilobed extruded body with a length of 4000 mm and an estimated pressure drop of 0.08 bar / m. B2 is a 1 / 16-inch cylindrical extruded body with a length of 3000 mm and an estimated pressure drop of 0.15 bar / m. B3 is a 1 / 8-inch trilobed extruded body with a length of 4000 mm and an estimated pressure drop of 0.08 bar / m at B1. To hold the 150 mm extruded body layer C, inert ceramic balls are placed on a catalyst support that holds all layers (A, B1, B2, C) and above a quenching section (totaling 370 mm, including a bubble cap mixing zone and a void zone) that receives cooling hydrogen. Below the mixing zone, two more inert layers totaling 300 mm are placed: an inert tablet-shaped material layer to fix the lower layers and ensure initial distribution, and another inert material layer to further distribute the flow and capture impurities. Below these layers, two more layers of active hydrocracking catalysts F1, F2, and F3 are placed. F1 is a 1 / 8-inch tri-lobed extruded body 4000 mm with an estimated pressure drop of 0.12 bar / m, F2 is a 1 / 12-inch quad-lobed extruded body 3000 mm with an estimated pressure drop of 0.18 bar / m, and F3 is a 1 / 8-inch tri-lobed extruded body 4000 mm with an estimated pressure drop of 0.12 bar / m. Subsequently, a 1350 mm hydrogenated finish catalyst (1 / 20 inch trilobed) layer (G) is placed, and three different sizes of inert ceramic balls (1200 mm) placed on a catalyst support are positioned in front of the hold-down layer H.

[0056] Compared to the embodiment in Figure 1, this embodiment may be more complex due to the additional layer, but it has lower pressure loss and can provide a more uniform flow throughout the three layers through intermediate redistribution.

[0057] Figure 3 Figure 3 shows an example of catalyst loading at the bottom of a reactor based on prior art. The top of the tower is a void, followed by an inert material layer (A) to fix the lower layers and ensure initial distribution. The total height of A is 300 mm. Below this layer is a single layer of activated hydrogenation catalyst B. B is an 11,000 mm 1 / 12 inch tri-lobed extruded body, with an estimated pressure drop of 0.1 bar / m. To hold the 150 mm extruded body layer C, an inert ceramic ball layer is placed on the catalyst support. This support holds all layers (A, B1, B2, C) and is located above the quenching zone (totaling 370 mm, including the bubble cap mixing zone and void zone) that receives the cooling hydrogen. Below the mixing zone are two more inert layers totaling 300 mm: an inert tablet-shaped material layer to fix the lower layers and ensure initial distribution, and another inert material layer to further distribute the flow and capture impurities. Below these layers, two more layers of active hydrogenocrack catalyst F are placed. F is an 11,000 mm 1 / 10 inch tri-lobed extruded body with an estimated pressure drop of 0.14 bar / m. Subsequently, a 1,350 mm layer (G) of hydrogenation finish catalyst (1 / 20 inch tri-lobed) is placed, and prior to that, a 1,200 mm hold-down layer H of inert ceramic balls of three different sizes placed on a catalyst support is placed.

[0058] Figure 4 Figure 4 shows the thermal performance of the two beds in the reactor according to the present invention, both of which are effective for exothermic hydrocracking. The reactor has two main beds (11 m hydrocracking beds (B; B1 + B2) and 11 m hydrocracking beds (F; F1 + F2)) on which smaller beds are arranged. The two hydrocracking beds are configured as shown in Figure 1, with the first bed having (B1) a 1 / 8-inch trilobed hydrocracking catalyst of 5500 mm placed on top of (B2) a 1 / 16-inch cylindrical hydrocracking catalyst of 5500 mm, and the second bed having (F1) a 1 / 8-inch trilobed hydrocracking catalyst of 5500 mm placed on top of (F2) a 1 / 12-inch quadruped hydrocracking catalyst of 5500 mm. The average axial temperature rise in the first floor was 27°C and the pressure loss was 2.66 bar, distributed as 0.93 bar (0.08 bar / m) in B1 and 1.74 bar (0.16 bar / m) in B2. The average axial temperature rise in the second floor was 25°C and the pressure loss was 3.32 bar, distributed as 1.30 bar (0.12 bar / m) in F1 and 2.01 bar (0.18 bar / m) in F2.

[0059] The Y-axis in Figure 4 represents the radial temperature difference (dT) across the reactor. rad The temperature is shown in degrees Celsius, and the X-axis represents the radial temperature difference (dT) across the reactor. rad ) and the temperature difference (dT) across the layer in the axial direction. ax ) ratio (dT rad / dT ax The values ​​are shown in percentage units. An open symbol indicates the daily value for bed 1 (C), and a closed symbol indicates the daily value for bed 2 (I). In both cases, the initial stabilization period is omitted, and the following 140 days are shown. [Examples]

[0060] example When the hydrocracking reactor was loaded according to the scheme in Figure 1, a radial temperature deviation of XX°C was observed in bed C over 140 days, as shown in Figure 4. Similarly, the radial temperature deviation of XX°C in bed I, as shown in Figure 1, is shown in Figure 4.

[0061] At floor C, the mean radial temperature span was 4.3°C, corresponding to 16% of the axial temperature rise, while at floor I, the mean radial temperature span was 8.0°C, corresponding to 32% of the axial temperature rise. Both values ​​indicate good distribution, and the current radial temperature span is approximately half of the previous performance, shown by the two ellipses. The previous performance was obtained in a reactor loaded with an intermediate redistribution layer, where redistribution was not considered satisfactory, while the total pressure loss at each floor was slightly lower.

[0062] The results in this example demonstrate that by using fine particles to moderately increase pressure loss, it is possible to improve flow and temperature distribution within the reactor bed, leading to more stable operation and potentially extended catalyst life.

[0063] Patent Documents U.S. Patent No. 3732078 U.S. Patent No. 9732774

Claims

1. A reactor having an inlet above the outlet, wherein the pressure loss per meter is measured in the following order from the inlet to the outlet: dpm １ A first material layer that provides flow resistance equivalent to a pressure loss per meter dpm ２ The catalyst bed includes a plurality of material layers in the order of a second material layer that provides flow resistance equivalent to, Here, The combined height of the first and second layers is at least 4 m, the height of the second layer is at least 0.5 m, and the pressure loss per meter of the second layer is dpm ２ The pressure loss per meter of the first layer is dpm １ The reactor is at least 20% larger, and the first layer, the second layer, and any further layers are supported by a single catalyst support.

2. Located below the second layer, with a pressure loss of dpm per meter. ３ The reactor according to claim 1, further comprising a third layer of porous material that provides flow resistance equivalent to a pressure drop of at least 20%, wherein the material of the third layer comprises a porous heat-resistant support and a catalytically active metal, wherein the pressure drop per meter of the second layer is at least 20% greater than the pressure drop per meter provided by the third layer.

3. The reactor according to claim 1 or 2, wherein the material of the first layer, the material of the second layer, or, if present, the material of the third layer, for example, the material of several or all of these layers, comprises a porous heat-resistant support and a catalytically active metal.

4. The reactor according to any one of claims 1 to 3, wherein the shape of the reactor is substantially vertically cylindrical and the ratio of the height to the diameter of the first layer is less than 4:

1.

5. The reactor according to any one of claims 1 to 4, wherein the shape of the reactor is substantially vertically cylindrical, and the ratio of the total height to diameter of the first layer, the second layer, and, if present, the third layer of porous material is greater than 4:1, for example 5:1 or 6:

1.

6. The reactor according to any one of claims 1 to 5, wherein the shape of the reactor is substantially vertical cylindrical, and the ratio of the total height to diameter of the first layer, the second layer, and, if present, the third layer of porous material is less than 10:1, for example, 8:1 or 7:

1.

7. The reactor according to any one of claims 1 to 6, wherein at least 50% of the porous material of at least one of the first layer, the second layer, and the third layer, if present, has an average dimension along the shortest axis of 0.1 mm to 0.5 mm or 1 mm to 3 mm or 5 mm, and the ratio of the average dimension in the longest axis direction to the average dimension in the shortest axis direction is 1:1 to 20:

1.

8. The reactor according to any one of claims 1 to 7, wherein at least 50% of the porous material of the first layer, the second layer, and the third layer, if present, for example, multiple or all of these layers, has a tetrahedron, trihedron, annular, or cylindrical shape.

9. The reactor according to any one of claims 1 to 8, wherein at least one of the first layer, the second layer, and the third layer, if present, for example, at least 50% of the porous material of multiple or all of these layers is an extruded material.

10. The reactor according to any one of claims 1 to 9, wherein the mass concentrations of each catalytically active metal in the material of the first layer, the material of the second layer, and the material of the third layer, if present, differ by less than 20% of the total mass concentration of catalytically active metals, but the zones differ in size or shape.

11. The reactor according to any one of claims 1 to 10, wherein the catalytically active metal of the material in zone 1 and the material in zone 2, or the material in zone 3, if present, is active in hydrocracking, and optionally comprises a zeolite or molecular sieve.

12. A method for fluid redistribution in a fixed-bed reactor having a liquid inlet above a liquid outlet, comprising the step of providing a first material layer disposed on a second material layer in a single-bed support made of a single catalyst support, wherein the combined height of the first material layer and the second material layer is at least 4 m, the height of the second layer is at least 0.5 m, and the pressure loss per meter in the second material layer is at least 20% higher than the pressure loss per meter in the first material layer.

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