Turbulent fluidized bed reaction device and turbulent fluidized bed reaction method using same

Abstract

The invention relates to the technical field of reactor design, and provides a turbulent fluidized bed reaction device and a turbulent fluidized bed reaction method using the same, the turbulent fluidized bed reaction device comprises a shell, the shell comprises a reaction chamber and an outlet pipe; the turbulent fluidized bed reaction device comprises a guide cylinder arranged in the reaction cavity; the outlet pipe is arranged on one side of the upper part of the reaction cavity; and the height-diameter ratio of the reaction cavity is (0.1-1): 1. By designing the reaction cavity with a low height-diameter ratio and synchronously installing the guide cylinder, the particle flux of a catalyst can be improved, and the defect that the particle flux of a turbulent fluidized bed in a traditional industrial reactor is low is overcome.

Description

Technical Field

[0001] The present invention relates to the field of reactor technology, and in particular to a turbulent fluidized bed reaction device and a turbulent fluidized bed reaction method using the same. Background Art

[0002] The turbulent fluidized bed reactor has the advantages of strong gas-solid contact, high efficiency of heat and mass transfer, and long gas-solid residence time due to the strong interaction between solid particles and small bubbles. However, due to its low particle flux and severe gas-solid backmixing, it is difficult to adapt to the needs of industrial production development.

[0003] In recent years, researchers have discovered a new type of turbulent fluidized bed, the circulating turbulent fluidized bed (CTFB), through the method of secondary air intake. The results show that under the operating conditions of the superficial gas velocity of 1m / s, the axial solid content of the circulating turbulent fluidized bed is uniformly distributed, and the particle flux is 150kg / m 2 s.

[0004] Therefore, it is of great significance to design a high-throughput turbulent fluidized bed reactor to meet the needs of industrial reactors. Summary of the invention

[0005] In view of the shortcomings of the prior art, the purpose of the present invention is to provide a turbulent fluidized bed reaction device and a turbulent fluidized bed reaction method using the same. By designing a guide tube and controlling a reaction chamber with a low aspect ratio, a turbulent fluidized bed with a high particle flux can be obtained, which meets the needs of industrial reactors and has broad application prospects.

[0006] To achieve this object, the present invention adopts the following technical solutions:

[0007] In a first aspect, the present invention provides a turbulent fluidized bed reaction device, comprising a shell, the shell comprising a reaction chamber and an outlet pipe; the turbulent fluidized bed reaction device comprises a guide tube arranged inside the reaction chamber; the outlet pipe is arranged on one side of the upper part of the reaction chamber; the height-to-diameter ratio of the reaction chamber is 0.1 to 1:1.

[0008] The turbulent fluidized bed reaction device provided by the present invention can have a high particle flux under the condition of turbulent flow, thereby solving the problem that it is difficult to obtain a turbulent flow reactor with a high particle flux in the prior art.

[0009] The turbulent fluidized bed reaction device of the present invention has the following characteristics: first, the present invention reduces the aspect ratio to 0.1-1:1, and this relatively low aspect ratio has the advantages of improving fluidization quality and increasing heat and mass transfer efficiency; at the same time, a guide tube is arranged inside the reaction chamber, thereby increasing the gas velocity inside the guide tube and increasing the particle flux, and an annular gap is provided between the guide tube and the reaction chamber, so that during the reaction process, a moderate gas velocity can be maintained in the entire reaction chamber while maintaining a relatively high particle flux, thereby ultimately achieving the effect of increasing the yield.

[0010] Specifically, the height-to-diameter ratio of the reaction chamber is 0.1 to 1:1, for example, it can be 0.1:1, 0.2:1, 0.3:1, 0.4:1, 0.5:1, 0.6:1, 0.7:1, 0.8:1, 0.9:1 or 1:1, but is not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0011] It is worth noting that when the height-to-diameter ratio of the reaction chamber is too high, there will be a dead zone inside the reactor, resulting in a poor reaction effect.

[0012] Preferably, the reaction chamber is divided into an entrainment zone, an elutriation zone and a dense phase zone from top to bottom according to the change dE / dH of the particle flux E with the height of the reaction chamber, and the outlet pipe is arranged on the side of the entrainment zone; wherein the change dE / dH of the particle flux E in the elutriation zone with the height of the reaction chamber is ≤0.05kg / (m 3 ·s).

[0013] Preferably, the particle flux is defined as Where E is the particle flux, in kg / (m 2 ·s); ρ s is the particle density, in kg / m 3 ; A i is the cross-sectional area of ​​each grid, in m 2 ; A is the cross-sectional area of ​​the reactor, in m 2 ; is the velocity of the particle in the z direction; the unit is m / s.

[0014] It is worth mentioning that there are two key points in the design of the reaction chamber in the present invention. The first is the location of the outlet pipe. The location of the outlet pipe has a significant impact on the residence time of the reaction and the effect of the reaction. By setting the outlet pipe in the segregation zone, the particle flux begins to decrease exponentially at this time. The particle flux of the reaction chamber in this area is low, and the reaction efficiency is already low. That is, setting the outlet pipe in the segregation zone can better improve the effect of the reaction. However, for a turbulent fluidized bed with a high particle flux, the prediction accuracy of the segregation zone section is not high, which makes it difficult to determine the location of the outlet pipe. In this regard, the inventor has found through research that, based on the definition of traditional particle flux, considering the net upward velocity of the particles is more conducive to improving the prediction accuracy of the particle flux. The particle flux value obtained based on the above-mentioned particle flux definition is more in line with the actual situation, and can ultimately better predict the section positions of the entrainment zone, the segregation zone, and the dense phase zone.

[0015] Preferably, the diameter of the outlet pipe is 100 mm to 2000 mm, for example, it can be 100 mm, 312 mm, 523 mm, 734 mm, 945 mm, 1156 mm, 1367 mm, 1578 mm, 1789 mm or 2000 mm, but is not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0016] Preferably, the ratio of the diameter of the guide tube to the diameter of the reaction chamber is 0.4 to 0.7:1, for example, it can be 0.4:1, 0.44:1, 0.47:1, 0.5:1, 0.54:1, 0.57:1, 0.6:1, 0.64:1, 0.67:1 or 0.7:1, but is not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0017] Preferably, the ratio of the height of the guide tube to the height of the reaction chamber is 0.3 to 0.7:1, for example, it can be 0.3:1, 0.35:1, 0.39:1, 0.44:1, 0.48:1, 0.53:1, 0.57:1, 0.62:1, 0.66:1 or 0.7:1, but is not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0018] Preferably, the height-to-diameter ratio of the guide tube is 0.4-0.7, for example, it may be 0.4, 0.44, 0.47, 0.5, 0.54, 0.57, 0.6, 0.64, 0.67 or 0.7, but is not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0019] Furthermore, the size of the draft tube and the initial particle stacking height are important design parameters of the turbulent fluidized bed reactor, and both parameters have a great influence on the reactor performance. Therefore, determining the draft tube and the initial particle stacking height is very critical to the design of the turbulent fluidized bed reactor, which directly affects the product yield and catalyst particle flux obtained in the industrial reactor.

[0020] Experimental tests can intuitively show the influence of the guide tube and the initial particle stacking height on the particle flux in the reactor. However, direct testing takes a long time and has high economic costs, and it is difficult to obtain important factors such as the flux and solid content of each part of the reactor through experiments. In the actual optimization and amplification process, these parameters play an important reference role. The CFD numerical simulation method can solve these problems well. Through CFD numerical simulation, the flow environment of the turbulent fluidized bed reactor under the corresponding working conditions can be studied by changing the design parameters of the guide tube and the initial particle stacking height, and the particle flux and solid content distribution of each cross section can be calculated, so as to design a high-throughput turbulent fluidized bed reactor, thereby reducing the economic cost and providing a theoretical basis for industrial testing.

[0021] The present invention adopts 2.4 Mesh the reactor structure and simulate using 17.0 was used as the solver to perform numerical simulation of gas-solid two-phase flow. First, the effects of different initial particle stacking heights on the reactor flux were compared. After determining the optimal initial particle stacking height, a guide tube was added inside the reactor. The changes in particle flux with and without the guide tube in the reactor were compared, and the initial particle stacking height and guide tube size of the high-throughput turbulent fluidized bed reactor were determined.

[0022] And through research, it is found that the size of the guide tube and the initial particle stacking height calculated by the self-defined particle flux definition formula of the present invention have a better reaction effect. After design, when the size of the guide tube is designed within the above range, it has the best reaction conversion rate and yield, and the particle flux is large while maintaining turbulent flow.

[0023] Preferably, the turbulent fluidized bed reaction device further comprises a gas phase distributor arranged at the bottom of the reaction chamber, and a plurality of openings are distributed on the gas phase distributor.

[0024] Preferably, the porosity of the gas phase distributor is 5-15%, for example, it can be 5%, 6%, 7%, 8%, 9%, 10%, 11%, 12%, 13%, 14% or 15%, etc., but is not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0025] Preferably, the aperture of the opening on the gas phase distributor is 75 to 150 mm, for example, it can be 75 mm, 80 mm, 85 mm, 90 mm, 100 mm, 120 mm, 130 mm, 135 mm, 140 mm or 150 mm, but is not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0026] Preferably, the shell further comprises a transition zone and a gas phase inlet which are sequentially connected to the bottom of the reaction chamber.

[0027] Preferably, the transition zone is funnel-shaped, and the angle between the wall of the transition zone and the wall of the reaction chamber is 30-60°, for example, it can be 30°, 32°, 35°, 38°, 40°, 42°, 45°, 50°, 52°, 55° or 60°, but is not limited to the listed values, and other values ​​not listed within the range are also applicable.

[0028] Preferably, the turbulent fluidized bed reaction device further comprises a catalyst circulation inlet, and the catalyst circulation inlet is arranged at the side of the dense phase zone in the reaction chamber.

[0029] Preferably, the opening diameter of the catalyst circulation inlet is 100-1000 mm, for example, it can be 100 mm, 200 mm, 300 mm, 400 mm, 500 mm, 600 mm, 700 mm, 800 mm, 900 mm or 1000 mm, but is not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0030] In a second aspect, the present invention provides a turbulent fluidized bed reaction method, which is carried out using the turbulent fluidized bed reaction apparatus described in the first aspect.

[0031] Preferably, the turbulent fluidized bed reaction method comprises: arranging catalyst particles on a gas phase distributor, and introducing a gas phase to carry out a reaction under turbulent flow.

[0032] Preferably, the particle size of the catalyst is 50-100 μm, for example, 50 μm, 56 μm, 62 μm, 67 μm, 73 μm, 78 μm, 84 μm, 89 μm, 95 μm or 100 μm, but is not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0033] Preferably, the density of the catalyst is 1000-1600 kg / m 3 , for example, it can be 1000kg / m 3 , 1060kg / m 3 、1130kg / m 3 , 1200kg / m 3、1260kg / m 3 、1330kg / m 3 , 1400kg / m 3 、1460kg / m 3 、1530kg / m 3 or 1600kg / m 3 The above values ​​are not limited to the above values, and other values ​​not listed in the above values ​​are also applicable.

[0034] Preferably, the ratio of the pre-loading height of the catalyst on the gas phase distributor to the diameter of the reaction chamber is 0.1 to 0.5, for example, it can be 0.1, 0.15, 0.19, 0.24, 0.28, 0.33, 0.37, 0.42, 0.46 or 0.5, but is not limited to the listed values, and other unlisted values ​​within this range are also applicable.

[0035] Through research, it was found that when the ratio of the pre-loading height of the catalyst to the diameter of the reaction chamber is within the above range, not only can the effect of turbulent flow be achieved, but also a high particle flux can be achieved at the same time. When the ratio of the pre-loading height to the diameter of the reaction chamber is too small, there are problems such as low particle concentration, low flux, and insufficient gas-solid contact. When the ratio of the pre-loading height to the diameter of the reaction chamber is too large, there is a problem of severe grinding of the inner wall of the reactor.

[0036] Preferably, the particle flux of the dense phase zone is 300-400 kg / (m 2 ·s), for example, it can be 300kg / (m 2 ·s)、312kg / (m 2 ·s)、323kg / (m 2 ·s)、334kg / (m 2 ·s)、345kg / (m 2 ·s)、356kg / (m 2 ·s)、367kg / (m 2 ·s)、378kg / (m 2 ·s)、389kg / (m 2 ·s) or 400kg / (m 2 ·s), etc., but not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0037] Preferably, the particle flux of the entrainment zone is 20 to 300 kg / (m 2 ·s), for example, it can be 20kg / (m 2 ·s)、52kg / (m 2 ·s)、83kg / (m 2 ·s)、114kg / (m 2·s)、145kg / (m 2 ·s)、176kg / (m 2 ·s)、207kg / (m 2 ·s)、238kg / (m 2 ·s)、269kg / (m 2 ·s) or 300kg / (m 2 ·s), etc., but not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0038] Preferably, the gas velocity of the gas phase in the reaction chamber is 10 to 30 m / s, for example, it can be 10 m / s, 11 m / s, 12 m / s, 13 m / s, 14 m / s, 15 m / s, 16 m / s, 20 m / s, 22 m / s, 23 m / s, 26 m / s or 30 m / s, but is not limited to the listed values, and other values ​​not listed within the range are also applicable.

[0039] The present invention has no particular limitation on the specific reaction type in the above process, and a reaction type well known to those skilled in the art may be adopted, for example, it may be an olefin high temperature catalytic cracking process.

[0040] Experimental tests can intuitively show the influence of the guide tube and the initial particle stacking height on the particle flux in the reactor. However, direct testing takes a long time and has high economic costs, and it is difficult to obtain important factors such as the flux and solid content of each part of the reactor through experiments. In the actual optimization and amplification process, these parameters play an important reference role. The CFD numerical simulation method can solve these problems well. Through CFD numerical simulation, the flow environment of the turbulent fluidized bed reactor under the corresponding working conditions can be studied by changing the design parameters of the guide tube and the initial particle stacking height, and the particle flux and solid content distribution of each cross section can be calculated, so as to design a high-throughput turbulent fluidized bed reactor, thereby reducing the economic cost and providing a theoretical basis for industrial testing.

[0041] The present invention adopts 2.4 Mesh the reactor structure and simulate using 17.0 was used as the solver to perform numerical simulation of gas-solid two-phase flow. First, the effects of different initial particle stacking heights on the reactor flux were compared. After determining the optimal initial particle stacking height, a guide tube was added inside the reactor, and the changes in particle flux with and without the guide tube in the reactor were compared. The initial particle stacking height and guide tube size of the turbulent fluidized bed reactor were determined.

[0042] Specifically, the simulation process includes the following steps:

[0043] Step 1: Determine the structure, geometric dimensions, operating parameters and physical properties of the turbulent fluidized bed reactor; the geometric dimensions include the height and diameter of the reactor, the diameter of the draft tube, the height of the draft tube, the diameter and length of the outlet pipe, and the angle of the transition zone. The operating parameters include the superficial gas velocity of the reactor. The physical properties refer to the temperature, viscosity, pressure, composition and density of the fluidizing gas, and the particle size distribution and density of the solid particles.

[0044] Step 2: Establish the geometric model of the turbulent fluidized bed reactor, mesh the geometric model using a combination of structured and unstructured grids, select the Euler-Euler two-phase flow model, the laminar flow model as the viscosity model, and the EMMS-matrix model as the gas-solid drag model, and couple it with the FLUENT solver through a user-defined function (UDF).

[0045] Step 3: Define the material properties of the gas phase and solid phase, define the boundary conditions of the inlet and outlet and the wall, and the initial conditions of the calculation, define the solution parameters, define the particle flux, and use 17.0 is used as a solver to perform transient simulation first. After the detected variables maintain dynamic equilibrium, time-averaged statistics are performed to obtain time-averaged flow field data.

[0046] Step 4: Output the data obtained from the CFD simulation and display them as graphs and curves, and use Tecplot software for post-processing. Through post-processing, the simulation results can be intuitively observed and analyzed to obtain information such as the flow field inside the reactor, concentration distribution, particle flux distribution, and apparent gas velocity distribution.

[0047] Based on the research of gas-solid turbulent fluidized bed, the present invention further studies the influence of changing the initial particle stacking height on the particle flux and solid content distribution in the reactor, and greatly reduces the research cost compared with the experiment, providing a basis for technical improvement and optimization of reactor geometric parameters. Moreover, a guide tube is installed inside the reactor, and simulations show that the installation of the guide tube can increase the particle flux of the reactor by increasing the particle velocity inside the reactor.

[0048] Compared with the prior art, the present invention has at least the following beneficial effects:

[0049] The turbulent fluidized bed reaction device provided by the present invention can obtain high particle flux under suitable gas velocity conditions, improve the reaction conversion rate and reaction effect, is particularly suitable for olefin high-temperature catalytic cracking processes, and has broad application prospects. BRIEF DESCRIPTION OF THE DRAWINGS

[0050] Figure 1 This is the structural diagram of the high-throughput turbulent fluidized bed reactor.

[0051] Figure 2 Schematic diagram of mesh division.

[0052] Figure 3 It is the time-averaged axial solid content distribution diagram.

[0053] Figure 4 To compare the particle flux distribution along the reactor height at different initial particle stacking heights.

[0054] Figure 5 To compare the particle flux distribution along the reactor height with and without the guide tube in the reactor.

[0055] In the figure: 1. gas phase inlet; 2. transition zone; 3. reaction chamber; 4. gas phase distributor; 5. guide tube. DETAILED DESCRIPTION

[0056] For the convenience of understanding the present invention, the present invention lists the following embodiments. It should be understood by those skilled in the art that the embodiments are only to help understand the present invention and should not be regarded as specific limitations of the present invention.

[0057] It should be understood that, in the description of the present invention, the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", etc., indicating the orientation or position relationship are based on the orientation or position relationship shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present invention.

[0058] It should be noted that in the description of the present invention, unless otherwise clearly specified and limited, the terms "disposed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two elements. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood by specific circumstances.

[0059] Those skilled in the art should understand that the present invention necessarily includes necessary pipelines, conventional valves and general pump equipment for realizing a complete process, but the above content does not belong to the main inventive point of the present invention. Those skilled in the art can add layouts on their own based on the process flow and equipment structure selection, and the present invention does not make special requirements and specific limitations on this.

[0060] In order to facilitate experimental comparison, the following examples and comparative examples are simulated and analyzed using the following simulation process. Specifically, the simulation process includes:

[0061] (1)Use 2.4 Establish the geometric model of the reactor, perform meshing, and determine the number of meshes.

[0062] Reference Figure 1 , the geometric structure of the turbulent fluidized bed reactor, and the physical modeling of the turbulent fluidized bed reactor. When dividing the grid, the structured grid and the unstructured grid are combined to encrypt the grid of the gas distributor. The number of grids used is 220,000, and the grid model is as follows Figure 2 shown.

[0063] (2) Determine the model that describes the fluid flow in a turbulent fluidized bed reactor.

[0064] The gas-solid two phases are in full contact in the turbulent fluidized bed reactor. The Euler-Euler two-phase flow model is adopted, the laminar flow model is selected as the viscosity model, and the EMMS-matrix model is selected as the drag force between the gas and solid phases. It is coupled with the FLUENT solver through a user-defined function (UDF).

[0065] (3) Application 17.0 is used as the solver to set the physical parameters and inlet and outlet boundary conditions. A transient simulation is performed first. After the detected variables maintain dynamic equilibrium, time-averaged statistics are performed to obtain the time-averaged flow field.

[0066] According to the process conditions of the turbulent fluidized bed reactor, the gas phase inlet is the velocity inlet, the outlet is the pressure outlet, the wall is set to no slip, and the catalyst particles are pre-loaded in the initial turbulent fluidized bed reactor. The solution first uses transient calculation of the gas-solid two-phase flow, and the flow field is time-averaged after stabilization. The solution uses the Phase-coupled-SIMPLE algorithm, and each equation is solved using the second-order upwind format. The calculation time step is set to 0.0005s. After 40 instantaneous calculations, a 20s time-averaged statistics is performed. The particle flux is defined as:

[0067]

[0068] Where E is the particle flux, unit is kg / (m 2 ·s); ρ s is the particle density, in kg / m 3 ; A i is the cross-sectional area of ​​each grid, in m 2 ; A is the cross-sectional area of ​​the reactor, in m 2 ; is the velocity of the particle in the z direction; the unit is m / s.

[0069] (4) Post-process the calculation results and analyze the results of CFD numerical simulation.

[0070] Post-processing was performed using Tecplot software. Figure 3 The solid content distribution diagram obtained shows that most of the particles are gathered in the reaction chamber, and the particle concentration inside the guide tube is higher than that outside the guide tube.

[0071] Example 1

[0072] This embodiment provides a turbulent fluidized bed reaction device, which includes a shell, and the shell includes a reaction chamber and an outlet pipe; the turbulent fluidized bed reaction device includes a guide tube arranged inside the reaction chamber.

[0073] The outlet pipe is arranged on one side of the upper part of the reaction chamber; the height-to-diameter ratio of the reaction chamber is 0.5:1. The reaction chamber is divided into an entrainment zone, an elutriation zone and a dense phase zone from top to bottom according to the change dE / dH of the particle flux E with the height of the reaction chamber, and the outlet pipe is arranged on the side of the entrainment zone; wherein the change dE / dH of the particle flux E in the elutriation zone with the height of the reaction chamber is ≤0.05kg / (m 3 ·s).

[0074] The particle flux is defined as Where E is the particle flux, in kg / (m 2 ·s); ρ s is the particle density, in kg / m 3 ; A i is the cross-sectional area of ​​each grid, in m 2 ; A is the cross-sectional area of ​​the reactor, in m 2 ; is the velocity of the particle in the z direction; the unit is m / s.

[0075] The diameter of the outlet pipe is 500 mm. The ratio of the diameter of the guide tube to the diameter of the reaction chamber is 0.5:1; the ratio of the height of the guide tube to the height of the reaction chamber is 0.6:1; and the height-to-diameter ratio of the guide tube is 0.5.

[0076] The turbulent fluidized bed reaction device also includes a gas phase distributor arranged at the bottom of the reaction chamber, and a plurality of openings are distributed on the gas phase distributor; the opening rate of the gas phase distributor is 10%; and the aperture of the opening on the gas phase distributor is 100 mm.

[0077] The shell also includes a transition zone and a gas phase inlet which are sequentially connected to the bottom of the reaction chamber; the transition zone is funnel-shaped, and the angle between the wall of the transition zone and the wall of the reaction chamber is 45°; the turbulent fluidized bed reaction device also includes a catalyst circulation inlet, which is arranged on the side of the dense phase zone in the reaction chamber; the opening diameter of the catalyst circulation inlet is 600 mm.

[0078] Example 2

[0079] This embodiment provides a turbulent fluidized bed reaction device, which includes a shell, and the shell includes a reaction chamber and an outlet pipe; the turbulent fluidized bed reaction device includes a guide tube arranged inside the reaction chamber.

[0080] The outlet pipe is arranged on one side of the upper part of the reaction chamber; the height-to-diameter ratio of the reaction chamber is 0.1:1. The reaction chamber is divided into an entrainment zone, an elutriation zone and a dense phase zone from top to bottom according to the change dE / dH of the particle flux E with the height of the reaction chamber, and the outlet pipe is arranged on the side of the entrainment zone; wherein the change dE / dH of the particle flux E in the elutriation zone with the height of the reaction chamber is ≤0.05kg / (m 3 ·s).

[0081] The particle flux is defined as Where E is the particle flux, in kg / (m 2 ·s); ρ s is the particle density, in kg / m 3 ; A i is the cross-sectional area of ​​each grid, in m 2 ; A is the cross-sectional area of ​​the reactor, in m 2 ; is the velocity of the particle in the z direction; the unit is m / s.

[0082] The diameter of the outlet pipe is 100 mm. The ratio of the diameter of the guide tube to the diameter of the reaction chamber is 0.4:1; the ratio of the height of the guide tube to the height of the reaction chamber is 0.7:1; and the height-to-diameter ratio of the guide tube is 0.4.

[0083] The turbulent fluidized bed reaction device also includes a gas phase distributor arranged at the bottom of the reaction chamber, and a plurality of openings are distributed on the gas phase distributor; the opening rate of the gas phase distributor is 15%; and the aperture of the openings on the gas phase distributor is 75 mm.

[0084] The shell also includes a transition zone and a gas phase inlet which are sequentially connected to the bottom of the reaction chamber; the transition zone is funnel-shaped, and the angle between the wall of the transition zone and the wall of the reaction chamber is 30°; the turbulent fluidized bed reaction device also includes a catalyst circulation inlet, which is arranged on the side of the dense phase zone in the reaction chamber; the opening diameter of the catalyst circulation inlet is 1000mm.

[0085] Example 3

[0086] This embodiment provides a turbulent fluidized bed reaction device, which includes a shell, and the shell includes a reaction chamber and an outlet pipe; the turbulent fluidized bed reaction device includes a guide tube arranged inside the reaction chamber.

[0087] The outlet pipe is arranged on one side of the upper part of the reaction chamber; the height-to-diameter ratio of the reaction chamber is 1:1. The reaction chamber is divided into an entrainment zone, an elutriation zone and a dense phase zone from top to bottom according to the change dE / dH of the particle flux E with the height of the reaction chamber, and the outlet pipe is arranged on the side of the entrainment zone; wherein the change dE / dH of the particle flux E in the elutriation zone with the height of the reaction chamber is ≤0.05kg / (m 3 ·s).

[0088] The particle flux is defined as Where E is the particle flux, in kg / (m 2 ·s); ρ s is the particle density, in kg / m 3 ; A i is the cross-sectional area of ​​each grid, in m 2 ; A is the cross-sectional area of ​​the reactor, in m 2 ; is the velocity of the particle in the z direction; the unit is m / s.

[0089] The diameter of the outlet pipe is 2000 mm. The ratio of the diameter of the guide tube to the diameter of the reaction chamber is 0.7:1; the ratio of the height of the guide tube to the height of the reaction chamber is 0.3:1; and the height-to-diameter ratio of the guide tube is 0.7.

[0090] The turbulent fluidized bed reaction device also includes a gas phase distributor arranged at the bottom of the reaction chamber, and a plurality of openings are distributed on the gas phase distributor; the opening rate of the gas phase distributor is 5%; and the aperture of the openings on the gas phase distributor is 150 mm.

[0091] The shell also includes a transition zone and a gas phase inlet which are sequentially connected to the bottom of the reaction chamber; the transition zone is funnel-shaped, and the angle between the wall of the transition zone and the wall of the reaction chamber is 60°; the turbulent fluidized bed reaction device also includes a catalyst circulation inlet, which is arranged on the side of the dense phase zone in the reaction chamber; the opening diameter of the catalyst circulation inlet is 100 mm.

[0092] Example 4

[0093] This embodiment provides a turbulent fluidized bed reaction device. Except that the ratio of the diameter of the guide tube to the diameter of the reaction chamber is 0.3:1, the rest of the turbulent fluidized bed reaction device is the same as that of Embodiment 1, and will not be repeated here.

[0094] Example 5

[0095] This embodiment provides a turbulent fluidized bed reaction device. Except that the ratio of the diameter of the guide tube to the diameter of the reaction chamber is 0.8:1, the rest of the turbulent fluidized bed reaction device is the same as that of Embodiment 1, and will not be repeated here.

[0096] Example 6

[0097] This embodiment provides a turbulent fluidized bed reaction device. Except that the height-to-diameter ratio of the draft tube is 0.2, the rest of the turbulent fluidized bed reaction device is the same as that of Embodiment 1, and will not be described again.

[0098] Example 7

[0099] This embodiment provides a turbulent fluidized bed reaction device. Except that the height-to-diameter ratio of the draft tube is 0.8, the rest of the turbulent fluidized bed reaction device is the same as that of Embodiment 1, and will not be described again.

[0100] Example 8

[0101] This embodiment provides a turbulent fluidized bed reaction device, wherein the particle flux of the turbulent fluidized bed reaction device is defined as Except for this, the rest are the same as those in Example 1 and will not be described again.

[0102] Comparative Example 1

[0103] This comparative example provides a turbulent fluidized bed reaction device. Except that the guide tube is not provided, the rest of the turbulent fluidized bed reaction device is the same as Example 1, and will not be described again.

[0104] Comparative Example 2

[0105] This comparative example provides a turbulent fluidized bed reaction device. Except that the height-to-diameter ratio of the reaction chamber of the turbulent fluidized bed reaction device is 1.1:1, the rest is the same as that of Example 1, and no further details are given here.

[0106] Application Example 1

[0107] This application example provides a turbulent fluidized bed reaction method, which comprises the following steps:

[0108] Catalyst particles are arranged on the gas phase distributor, and the gas phase (pentene gas) is introduced to react under turbulent flow; the particle size D50 of the catalyst is 70 μm; the density of the catalyst is 1250 kg / m 3 ; The ratio of the pre-loading height of the catalyst on the gas phase distributor to the diameter of the reaction chamber is 0.4:1, and the gas velocity is 15m / s.

[0109] The ratios of different pre-filling heights to the diameter of the reaction chamber were set to 0.13, 0.26, and 0.40, respectively. Figure 4 It can be seen that as the ratio of the pre-filling height to the diameter of the reaction chamber gradually increases, within this range, the particle flux continues to increase.

[0110] Figure 5 The time-averaged particle flux axial distribution curves in Application Example 1 and Comparative Example 1 show that the curves of the two are roughly similar at the outlet pipe, while in the draft tube area, the particle flux of the reactor with the draft tube installed is significantly higher than that of the reactor without the draft tube installed. This shows that installing the draft tube can increase the particle velocity inside the reactor, thereby increasing the particle flux.

[0111] Application Example 2

[0112] This application example provides a turbulent fluidized bed reaction method, which comprises the following steps:

[0113] Catalyst particles are arranged on the gas phase distributor, and the gas phase (pentene gas) is introduced to react under turbulent flow; the particle size D50 of the catalyst is 50 μm; the density of the catalyst is 1600 kg / m 3 ; The ratio of the pre-loading height of the catalyst on the gas phase distributor to the diameter of the reaction chamber is 0.5:1, and the gas velocity is 30m / s.

[0114] Application Example 3

[0115] This application example provides a turbulent fluidized bed reaction method, which comprises the following steps:

[0116] Catalyst particles are arranged on a gas phase distributor, and a gas phase (pentene gas) is introduced to react under turbulent flow; the particle size D50 of the catalyst is 100 μm; the density of the catalyst is 1000 kg / m 3 ; The ratio of the pre-loading height of the catalyst on the gas phase distributor to the diameter of the reaction chamber is 0.1:1, and the gas velocity is 10m / s.

[0117] Application Examples 4 to 8 and Comparative Application Examples 1 to 3

[0118] Application Examples 4 to 8 and Application Comparative Examples 1 to 3 provide a turbulent fluidized bed reaction method. Except for using the turbulent fluidized bed reaction devices in Examples 4 to 8 and Comparative Examples 1 to 3 respectively, the rest of the turbulent fluidized bed reaction method is the same as Application Example 1, which will not be repeated here.

[0119] Application Example 9

[0120] This application example provides a turbulent fluidized bed reaction method. The turbulent fluidized bed reaction method is the same as Application Example 1 except that the ratio of the pre-loading height of the catalyst on the gas phase distributor to the diameter of the reaction chamber is 0.7:1, and will not be repeated here.

[0121] Application Example 10

[0122] This application example provides a turbulent fluidized bed reaction method. The turbulent fluidized bed reaction method is the same as Application Example 1 except that the ratio of the pre-loading height of the catalyst on the gas phase distributor to the diameter of the reaction chamber is 0.05:1, and is not described again.

[0123] The analysis results of the above application examples and comparative examples are shown in Table 1. The unit of particle flux is kg / (m 2 ·s), the unit of solid content is wt%. In the present invention, the solid content in the overall reaction chamber is preferably in the range of 0.20-0.35%, and preferably the solid content in the overall reaction chamber and the solid content of the guide tube are both in the range of 0.25-0.35%, at which time the turbulent flow can be maintained and the mass transfer and heat transfer efficiency are high.

[0124] Table 1

[0125]

[0126]

[0127] From Table 1, we can see the following points:

[0128] (1) It can be seen from the comprehensive application examples 1 to 3 that the turbulent fluidized bed reaction device provided by the present invention has a high particle flux, and the particle flux in the dense phase zone is 410 kg / (m 2 ·s), the solid content in the overall reaction chamber is above 0.28wt%, which greatly improves the reaction effect.

[0129] (2) In Application Example 4, the ratio of the diameter of the guide tube to the diameter of the reaction chamber is too small, the degree of back-mixing outside the guide tube is large, and the flow performance is reduced. Compared with Example 1, the particle flux is low, the degree of back-mixing is large, the solid content is high, but the particle velocity is low. In Application Example 5, the ratio of the diameter of the guide tube to the diameter of the reaction chamber is too high, which will increase the annular resistance and be unfavorable to the flow, reduce the working efficiency of the reactor, and cause problems such as uneven distribution of solid content and gas velocity. Compared with Example 1, the particle flux is low, the solid content is low, and the optimal effect cannot be achieved. This shows that the present invention controls the ratio of the diameter of the guide tube to the diameter of the reaction chamber within a reasonable range, which significantly improves the mass transfer effect.

[0130] (3) In Application Example 6, when the height-to-diameter ratio of the guide tube is too small, uneven flow will occur and the flow dead zone will increase, resulting in a decrease in the reaction rate and mass transfer rate. Compared with Example 1, only the particle flux in the guide tube area will be increased, resulting in a local increase in the particle flux of the guide tube, which will then drop rapidly, and the flux distribution will be uneven, which will not meet the requirements. In Application Example 7, when the height-to-diameter ratio of the guide tube is too high, it will affect the particle flow at the outlet pipe, thereby reducing the flow efficiency, the circulation distance is longer, and the resistance is increased. Compared with Example 1, the particle flux will be increased, the solid content will be reduced, and the apparent gas velocity will increase. This shows that the present invention preferably controls the height-to-diameter ratio of the guide tube within a reasonable range, which can better improve the mass transfer effect.

[0131] (4) The definition of particle flux in Application Example 8 is changed to In this case, the particle flux calculated by simulation is lower than that of Example 1, and the particle downward velocity is included in the flux, resulting in inaccurate calculation results. The particle flux and solid content data presented in the end are significantly reduced, which shows that the present invention has a better design result by preferably limiting the particle flux formula to the preferred formula of the present invention.

[0132] (5) It can be seen from Application Example 1 and Application Examples 9 to 10 that the turbulent fluidized bed reaction method provided by the present invention has a preferred setting range for the ratio of the pre-filling height to the diameter of the reaction chamber. When it is set within a reasonable range, a suitable solid content can be obtained under a high particle flux, thereby improving the mass transfer effect.

[0133] (6) When the turbulent fluidized bed reaction device in Comparative Example 1 is not provided with a draft tube, there are disadvantages such as low mass and heat transfer efficiency, difficulty in reactor enlargement, and uneven gas-solid flow. Compared with Example 1, the particle flux is significantly reduced. Although the solid content is high, the reaction uniformity is reduced. When the height-diameter ratio of the reaction chamber in Comparative Example 2 is high, there will be uneven solid content distribution, low heat and mass transfer efficiency, and low particle flux at the reactor outlet. Compared with Example 1, the particle flux of the reaction outlet pipe is greatly reduced.

[0134] The present invention illustrates the detailed features of the present invention through the above embodiments, but the present invention is not limited to the above detailed features, that is, it does not mean that the present invention must rely on the above detailed features to be implemented. Those skilled in the art should understand that any improvement to the present invention, equivalent replacement of the technical features selected by the present invention, addition of auxiliary technical features, selection of specific methods, etc., all fall within the protection scope and disclosure scope of the present invention.

Claims

1. A turbulent fluidized bed reaction device, characterized in that: The turbulent fluidized bed reaction device comprises a shell, and the shell comprises a reaction chamber and an outlet pipe; The turbulent fluidized bed reaction device comprises a guide tube arranged inside the reaction chamber; The outlet pipe is arranged on one side of the upper part of the reaction chamber; The height-to-diameter ratio of the reaction chamber is 0.1-1:

1.

2. The turbulent fluidized bed reaction device according to claim 1, characterized in that: The reaction chamber is divided into an entrainment zone, an elutriation zone and a dense phase zone from top to bottom according to the change dE / dH of the particle flux E with the height of the reaction chamber, and the outlet pipe is arranged on the side of the entrainment zone; Wherein, the particle flux E of the entrainment zone changes with the height of the reaction chamber dE / dH≤0.05kg / (m 3 ·s).

3. The turbulent fluidized bed reaction device according to claim 2, characterized in that: The particle flux is defined as Where E is the particle flux, in kg / (m 2 ·s); ρ s is the particle density, in kg / m 3 ; A i is the cross-sectional area of ​​each grid, in m 2 ; A is the cross-sectional area of ​​the reactor, in m 2 ; is the velocity of the particle in the z direction; the unit is m / s.

4. The turbulent fluidized bed reaction device according to any one of claims 1 to 3, characterized in that: The diameter of the outlet pipe is 100 mm to 2000 mm.

5. The turbulent fluidized bed reaction device according to any one of claims 1 to 4, characterized in that: The ratio of the diameter of the guide tube to the diameter of the reaction chamber is 0.4-0.7:1; Preferably, the ratio of the height of the guide tube to the height of the reaction chamber is 0.3-0.7:1; Preferably, the height-to-diameter ratio of the guide tube is 0.4-0.

7.

6. The turbulent fluidized bed reaction device according to any one of claims 1 to 5, characterized in that: The turbulent fluidized bed reaction device further comprises a gas phase distributor arranged at the bottom of the reaction chamber, and the gas phase distributor is provided with a plurality of openings; Preferably, the porosity of the gas phase distributor is 5 to 15%; Preferably, the aperture of the opening on the gas phase distributor is 75 to 150 mm.

7. The turbulent fluidized bed reaction device according to any one of claims 1 to 6, characterized in that: The housing further comprises a transition zone and a gas phase inlet which are sequentially connected to the bottom of the reaction chamber; Preferably, the transition zone is funnel-shaped, and the angle between the wall of the transition zone and the wall of the reaction chamber is 30-60°; Preferably, the turbulent fluidized bed reaction device further comprises a catalyst circulation inlet, and the catalyst circulation inlet is arranged at the side of the dense phase zone in the reaction chamber; Preferably, the opening diameter of the catalyst circulation inlet is 100 to 1000 mm.

8. A turbulent fluidized bed reaction method, characterized in that: The turbulent fluidized bed reaction method is carried out using the turbulent fluidized bed reaction device described in any one of claims 1 to 7.

9. The turbulent fluidized bed reaction method according to claim 8, characterized in that: The turbulent fluidized bed reaction method comprises: arranging catalyst particles on a gas phase distributor, and introducing a gas phase to react under turbulent flow; Preferably, the particle size of the catalyst is 50 to 100 μm; Preferably, the density of the catalyst is 1000-1600 kg / m 3 ; Preferably, the ratio of the pre-loading height of the catalyst on the gas phase distributor to the diameter of the reaction chamber is 0.1 to 0.

5.

10. The turbulent fluidized bed reaction method according to claim 9, characterized in that: The particle flux in the dense phase zone is 300-400 kg / (m 2 s); Preferably, the particle flux of the entrainment zone is 20 to 300 kg / (m 2 s); Preferably, the gas velocity of the gas phase in the reaction chamber is 10-30 m / s.

Images