Flow pattern judgment method and system of multiphase fluidized bed, electronic equipment and storage medium
By analyzing the operating fluid volume, gas volume and pressure drop data of the multiphase fluidized bed, we judge the flow transition point, and solving the problem of inaccurate judgment of the flow transition point in the prior art, achieving the optimal flow operation of the multiphase fluidized bed, optimizing product quality and operating safety.
Patent Information
- Application Number
- CN202311443049.X
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2023-11-01
- Publication Date
- 2025-05-06
AI Technical Summary
The prior art is difficult to accurately judge the transition point of flow type in industrial-scale multi-phase fluidized beds, resulting in operation within the non-optimal range, affecting production safety and product quality.
By obtaining the operating fluid volume, operating gas volume and pressure drop data of the multi-phase fluidized bed driving stage, converting it into apparent liquid speed and apparent gas speed, extracting the apparent gas speed and pressure drop data curves at the same apparent liquid speed, and using the sudden change point of the curve slope to determine the transition point between different flow types.
The accurate judgment of the flow transition point of the multi-phase fluidized bed is achieved, allowing the reactor to be in the optimal flow operation range by adjusting the gas and liquid volumes, thereby optimizing product quality and ensuring long-term operation.
Smart Images
Figure CN119935257A_ABST
Abstract
Description
Technical Field
[0001] The present invention relates to the technical field related to gas / liquid / solid multiphase fluidized beds, and in particular to a flow pattern determination method, system, electronic equipment and storage medium for a multiphase fluidized bed. Background Art
[0002] Gas / liquid / solid multiphase fluidized beds are widely used in the field of petrochemicals. Scale benefits and multi-energy coupling drive multiphase fluidized beds to develop in the direction of large-scale. However, the strong nonlinearity (diffusion term) and complex phase interactions (fourth-order tensors) of the fluid control equations make it very difficult to predict the phase distribution and phase transport properties under operating conditions; the amplification effect makes the dead zone, temperature difference, hot spots, coke formation, pressure drop and other problems in large fluidized beds more prominent, seriously affecting the safe production, product quality and long-term operation of the fluidized bed.
[0003] In a multiphase fluidized bed, different phase volume fluxes or different phase interface interaction forms will present different flow patterns in different scale equipment, and the same flow pattern has relatively similar phase distribution and transport properties in different scale equipment. By extracting the physical characteristics and transition conditions of different flow patterns from the complex multiphase flow process, we can not only better understand the evolution of various fluid mechanics parameters during the scale-up of multiphase flow equipment, but also design the optimal operating domain based on the characteristics of multiphase flow equipment.
[0004] There are three flow patterns in a multiphase fluidized bed. As the superficial gas and liquid velocities increase, the flow patterns generally appear in the order of uniform flow pattern, transition flow pattern and turbulent flow pattern. If the superficial liquid velocity is too small and the solid content is too high, or a low-resistance distributor is used, only the turbulent flow pattern will exist. There are large differences in the fluid mechanics properties of different flow patterns, and the best applicable processes are also very different. The uniform flow pattern has uniform bubble size distribution, low turbulence, and mild shear strength, which is suitable for some reactors with special requirements. For example, the bacterial cells of the bioreactor are fragile and suitable for reaction under mild shear strength; the boiling bed has requirements for the catalyst carryover and is not suitable for operation at high liquid velocity. For suspended beds or desulfurization, denitrification, and waste solid removal processes, it is more suitable to operate under turbulent flow patterns with high turbulence, fast phase interface renewal, and high mass transfer and heat transfer coefficients.
[0005] Due to the investment restrictions and production requirements of multiphase fluidized beds, multiphase fluidized beds operating in a uniform flow pattern tend to operate at the upper limit of the uniform flow pattern; due to the limitations of compressors or pumps, multiphase fluidized beds operating in a turbulent flow pattern tend to operate at the lower limit of the turbulent flow pattern. However, current literature and patents are unable to accurately give the criteria for the flow pattern transition point; since industrial-scale multiphase fluidized beds are opaque and generally only thermocouples and densitometers are set up in the fluidized bed, the method generally used in the literature to observe and measure the bed height to judge the flow pattern transition is no longer applicable to industrial equipment. Therefore, there is currently no effective method for judging the flow pattern transition point for industrial-scale multiphase fluidized beds.
[0006] The information disclosed in this background technology section is only intended to enhance the understanding of the overall background of the invention and should not be regarded as an acknowledgment or any form of suggestion that the information constitutes the prior art already known to a person skilled in the art. Summary of the invention
[0007] The object of the present invention is to provide a method and system for determining the flow pattern of a multiphase fluidized bed, which can accurately determine the transition point of the flow pattern through the curve relationship between the apparent gas velocity and the fluidized bed pressure drop under the same apparent liquid velocity conditions, and the operation is simple.
[0008] To achieve the above-mentioned purpose, according to the first aspect of the present invention, there is provided a method for determining the flow pattern of a multiphase fluidized bed, which is applicable to industrial-scale multiphase fluidized beds and comprises the following steps: A. obtaining operating liquid volume data that grows dynamically from zero to a target value during the start-up phase of the multiphase fluidized bed, and converting the operating liquid volume into an apparent liquid velocity; B. obtaining operating gas volume data that grows dynamically from zero to a target value during the start-up phase of the multiphase fluidized bed, and converting the operating gas volume into an apparent gas velocity; C. obtaining pressure drop data corresponding to the operating liquid volume and the operating gas volume during the start-up phase of the multiphase fluidized bed; D. extracting the curve of the apparent gas velocity and the pressure drop data of the multiphase fluidized bed at the same apparent liquid velocity, and judging the transition point between different flow patterns by the mutation point of the slope of the curve.
[0009] Furthermore, in the above technical solution, the different flow patterns in step D are respectively a uniform flow pattern, a transitional flow pattern and a turbulent flow pattern.
[0010] Furthermore, in the above technical solution, the conversion method of the apparent liquid velocity is as follows: l =q l / ρ l / A; among them, u l is the apparent liquid velocity, m / s; q l is the operating liquid volume, kg / s; ρ l is the density of the feed liquid phase, kg / m 3 , obtained from actual sampling analysis; A is the cross-sectional area of the fluidized bed reactor, m 2 .
[0011] Furthermore, in the above technical solution, the conversion method of the superficial gas velocity is as follows: g =q g / A; among them, u g is the superficial gas velocity, m / s; q g is the operating gas volume, m 3 / s; A is the cross-sectional area of the fluidized bed reactor, m 2 .
[0012] Furthermore, in the above technical solution, the operating liquid volume data may be 60% to 100% of the design value, and may be measured by the mass flow rate entering the fluidized bed.
[0013] Furthermore, in the above technical solution, the operating gas volume data can be adjusted according to different processes and can be measured by the volume flow entering the fluidized bed.
[0014] Furthermore, in the above technical solution, the pressure drop data can be obtained by subtracting the sampling data measured by the pressure transmitters arranged at the inlet and outlet of the fluidized bed.
[0015] Furthermore, in the above technical solution, the transition point between different flow patterns is specifically a transition point from a uniform flow pattern to a transition flow pattern, or a transition point from a transition flow pattern to a turbulent flow pattern.
[0016] Furthermore, in the above technical solution, the dynamic growth in step A and step B may adopt a step-by-step growth.
[0017] According to a second aspect of the present invention, the present invention provides a flow pattern determination system for a multiphase fluidized bed, comprising: an apparent liquid velocity acquisition module, which is used to obtain operating liquid volume data that dynamically grows from zero to a target value during the start-up phase of the multiphase fluidized bed, and convert the operating liquid volume into an apparent liquid velocity; an apparent gas velocity acquisition module, which is used to obtain operating gas volume data that dynamically grows from zero to a target value during the start-up phase of the multiphase fluidized bed, and convert the operating gas volume into an apparent gas velocity; a pressure drop data acquisition module, which is used to obtain pressure drop data corresponding to the operating liquid volume and the operating gas volume during the start-up phase of the multiphase fluidized bed; a flow pattern transition judgment module, which is used to extract the apparent gas velocity and the pressure drop data curve of the multiphase fluidized bed under the same apparent liquid velocity, and judge the transition point between different flow patterns through the mutation point of the slope of the curve.
[0018] According to the third aspect of the present invention, the present invention provides an electronic device for determining a flow type of a multiphase fluidized bed, comprising: at least one processor; and a memory communicatively connected to the at least one processor; wherein the memory stores instructions executable by the at least one processor, and the instructions are executed by the at least one processor so that the at least one processor executes a method for determining a flow type of a multiphase fluidized bed as described in any one of the above technical solutions.
[0019] According to a fourth aspect of the present invention, the present invention provides a non-transitory computer-readable storage medium, which stores computer-executable instructions, and the computer-executable instructions are used to enable a computer to execute a method for determining a flow pattern of a multiphase fluidized bed as described in any one of the above technical solutions.
[0020] Compared with the prior art, the present invention has one or more of the following beneficial effects:
[0021] 1) Based on the research findings that "the pressure drop of the bed can directly reflect the opening state of the distributor jet hole", the present invention further develops a flow pattern determination method for a multiphase fluidized bed of the present invention through a certain correlation between the two. The present invention can more accurately determine the transition points of three different flow patterns (i.e., uniform flow pattern, transitional flow pattern, and turbulent flow pattern) by using relatively easy-to-measure operating liquid volume, operating gas volume, and pressure drop data. These three parameters are parameters that must be monitored in real time in actual production of industrial-scale multiphase fluidized beds, and will not add additional measurement points and measurement costs;
[0022] 2) The present invention is aimed at an industrial-scale multiphase fluidized bed, and the reactor can be placed in the optimal flow pattern operating range by adjusting the gas and liquid amounts, so that production can be achieved under the optimal operating conditions, thereby optimizing product quality and ensuring long-term operation;
[0023] 3) Since the present invention only needs to obtain a series of apparent gas velocity, apparent liquid velocity and fluidized bed pressure drop data, the flow pattern transition of the multiphase fluidized bed can be effectively judged. The flow rate and pressure drop are both conventional measurement parameters with high measurement accuracy. The error of the obtained apparent gas velocity-fluidized bed pressure drop curve is small, and it is easy to accurately judge the transition point of the flow pattern.
[0024] The above description is only an overview of the technical solution of the present invention. In order to more clearly understand the technical means of the present invention and implement it according to the contents of the specification, and to make the above and other purposes, technical features and advantages of the present invention easier to understand, one or more preferred embodiments are listed below and described in detail with the accompanying drawings as follows. BRIEF DESCRIPTION OF THE DRAWINGS
[0025] Figure 1 It is a schematic flow chart of the flow pattern determination method of a multiphase fluidized bed according to the present invention.
[0026] Figure 2 It is a schematic diagram of the configuration of a porous nozzle distributor capable of producing uniform flow, transitional flow and turbulent flow patterns in a multiphase fluidized bed of the present invention.
[0027] Figure 3 It is a schematic diagram of the superficial gas velocity-fluidized bed pressure drop curve of Example 1 of the flow pattern determination method of the multiphase fluidized bed of the present invention.
[0028] Figure 4 It is a schematic diagram of the superficial gas velocity-fluidized bed pressure drop curve of Example 2 of the flow pattern determination method of the multiphase fluidized bed of the present invention.
[0029] Figure 5 It is a schematic diagram of the structure of the flow pattern determination system of the multiphase fluidized bed of the present invention.
[0030] Figure 6 It is a schematic diagram of the hardware structure of the electronic device for determining the flow pattern of the multiphase fluidized bed of the present invention. DETAILED DESCRIPTION
[0031] The specific implementation modes of the present invention are described in detail below in conjunction with the accompanying drawings, but it should be understood that the protection scope of the present invention is not limited by the specific implementation modes.
[0032] Unless explicitly stated otherwise, throughout the specification and claims, the term “comprise” or variations such as “include” or “comprising”, etc., will be understood to include the stated elements or components but not to exclude other elements or components.
[0033] In this document, for the convenience of description, spatial relative terms such as "below", "below", "down", "above", "above", "upper", etc. may be used to describe the relationship between one element or feature and another element or feature in the accompanying drawings. It should be understood that the spatial relative terms are intended to include different orientations of the object in use or operation in addition to the orientation depicted in the figure. For example, if the object in the figure is turned over, the element described as being "below" or "below" other elements or features will be oriented "above" the element or feature. Therefore, the exemplary term "below" can include both the below and above directions. Objects may also have other orientations (rotated 90 degrees or other orientations) and the spatial relative terms used in this document should be interpreted accordingly.
[0034] In this document, the terms "first", "second", etc. are used to distinguish two different elements or parts, and are not used to limit a specific position or relative relationship. In other words, in some embodiments, the terms "first", "second", etc. can also be interchangeable.
[0035] The method, system, electronic device and storage medium of the present invention are described in more detail below by way of specific embodiments. It should be understood that the embodiments are merely exemplary and the present invention is not limited thereto.
[0036] The inventor has found through research that the flow pattern in the fluidized bed is directly related to the state of the distributor, especially for industrial-scale multiphase fluidized beds, the distributor directly determines the initial distribution of each phase, thereby affecting the flow pattern of the fluidized bed. Moreover, changes in external conditions such as gas volume, liquid volume, liquid phase viscosity, and solid content all change the flow pattern by changing the pressure drop of the distributor. In general, low-resistance distributors (such as single-hole nozzles and horizontal spider-web distributors) can only produce turbulent flow patterns; high-resistance distributors (such as porous nozzles and horizontal spider-web distributors) can produce three flow patterns. Pressure drop is a commonly used measurement method in industry, mainly used to monitor whether there is a blockage between two measuring points. But in fact, the pressure drop directly reflects the energy change of the fluid between the two measuring points. In a multiphase flow field, phase content, phase density, and local resistance can all cause changes in pressure drop. Specifically for the distributor, since the change of the jet hole (actual opening rate) will cause the change among the above three factors, the pressure drop of the bed can directly reflect the opening state of the jet hole of the distributor, that is, there is a certain relationship between the bed pressure drop and the effective opening area. Therefore, the bed pressure drop can be used to judge the opening state of the distributor, so as to adjust the gas and liquid volume in a targeted manner to put the reactor in the best flow type operation range.
[0037] Based on the above principle, that is, the pressure drop of the bed can directly reflect the opening state of the distributor jet holes, the inventor has studied the flow pattern determination method of the multiphase fluidized bed of the present invention through a certain correlation between the two. Through the relatively easy-to-measure operating liquid volume, operating gas volume and pressure drop data, the transition points of three different flow patterns (the different flow patterns are uniform flow pattern, transitional flow pattern and turbulent flow pattern) can be judged more accurately. Therefore, for industrial-scale multiphase fluidized beds, the reactor can be placed in the optimal flow pattern operating range by adjusting the gas and liquid volumes.
[0038] Example 1
[0039] like Figure 1 As shown, this embodiment provides a method for determining the flow pattern of a multiphase fluidized bed, which is applicable to an industrial-scale multiphase fluidized bed, and includes the following steps:
[0040] Step S101, obtain the operating liquid volume data that dynamically increases from zero to the target value during the start-up phase of the multiphase fluidized bed, and convert the operating liquid volume into the apparent liquid velocity. Specifically, the operating liquid volume is generally determined in the design phase, but in actual industrial production, the operating liquid volume may be reduced due to the influence of previous or subsequent devices. Generally, the actual operating liquid volume is 60% to 100% of the design value, which can be obtained based on the mass flow rate entering the reactor. During the start-up phase of the fluidized bed, the operating liquid volume will increase from 0 to the target value, and generally increase in steps. Furthermore, the measured operating liquid volume is converted into the apparent liquid velocity, and the conversion method of the apparent liquid velocity is as follows:
[0041] u l =q l / ρ l / A;
[0042] Among them, u l is the apparent liquid velocity, m / s; q l is the operating liquid volume, kg / s; ρ l is the density of the feed liquid phase, kg / m 3 , which can be obtained by actual sampling analysis; A is the cross-sectional area of the fluidized bed reactor, m 2 .
[0043] Step S102, obtain the operating gas volume data that dynamically increases from zero to the target value during the start-up phase of the multiphase fluidized bed, and convert the operating gas volume into the apparent gas velocity. Specifically, the operating gas volume can generally be adjusted, such as the circulating hydrogen volume of residual oil hydrogenation and the circulating oxygen volume of the bioreactor can be adjusted according to actual needs. The actual operating gas volume can be obtained based on the volume flow rate entering the reactor. During the start-up phase of the fluidized bed, the operating gas volume will also increase from 0 to the target value, and generally also increase in steps. Further, the obtained operating gas volume is converted into the apparent gas velocity, and the conversion method of the apparent gas velocity is as follows:
[0044] u g =q g / A;
[0045] Among them, u g is the superficial gas velocity, m / s; q g is the operating gas volume, m 3 / s; A is the cross-sectional area of the fluidized bed reactor, m 2 .
[0046] Step S103, obtaining the pressure drop data corresponding to the operating liquid volume and the operating gas volume during the start-up phase of the multiphase fluidized bed. Specifically, in industry, pressure measuring points are generally set at the inlet and outlet of the fluidized bed, and the pressure drop of the multiphase fluidized bed can be obtained by subtracting the sampling data of the inlet and outlet pressure transmitters. During the start-up phase of the fluidized bed, since the operating liquid volume and the operating gas volume will increase from 0 to the target value, and generally increase in a step-by-step manner, a series of data on the apparent liquid velocity, apparent gas velocity and fluidized bed pressure drop can be obtained.
[0047] Step S104, extract the data curve of the superficial gas velocity and the pressure drop of the multiphase fluidized bed at the same superficial liquid velocity, and judge the transition point between different flow patterns by the mutation point of the curve slope. Specifically, in this embodiment, a drawing software (such as Excel, Origin, Matlab, etc.) can be used to draw the curve of the superficial gas velocity-fluidized bed pressure drop at the same superficial liquid velocity. According to the mutation of the curve slope, the transition point from the uniform flow pattern to the transition flow pattern, and the transition point from the transition flow pattern to the turbulent flow pattern can be obtained.
[0048] This embodiment only needs to obtain a series of data on superficial gas velocity, superficial liquid velocity and fluidized bed pressure drop to effectively judge the flow pattern transition of the multiphase fluidized bed. These three parameters are parameters that must be monitored in real time in the actual production of industrial-scale multiphase fluidized beds, and no additional measurement points and measurement costs will be added; and the flow rate and pressure drop are conventional measurement parameters with high measurement accuracy, and the curve error of the superficial gas velocity-fluidized bed pressure drop obtained is small, and it is easy to accurately judge the flow pattern transition point; in addition, the operating gas volume can generally be slightly adjusted according to production needs (≯20%), and the operating gas volume can be adjusted according to the flow pattern transition point judged in this embodiment (that is, the transition point from the uniform flow pattern to the transition flow pattern or the transition flow pattern to the turbulent flow pattern), so that production can be achieved under the optimal operating conditions, thereby optimizing product quality and ensuring long-term operation.
[0049] The following two examples further illustrate:
[0050] Example 1:
[0051] like Figure 2 As shown, a porous nozzle distributor 1 (forming bubbles 2 through the porous nozzle) is arranged in the multiphase fluidized bed 100, the fluidized bed diameter is 1.2 m, the solid content is 5% wt, and the operating liquid volume (apparent liquid velocity) is 0. The curve of the superficial gas velocity and the fluidized bed pressure drop is as shown in FIG. Figure 3 shown. Figure 3 The superficial gas velocity-fluidized bed pressure drop curve has a "platform" segment between the steep drop and the steep rise. The left end point of the "platform" segment corresponds to the transition point from the uniform flow pattern to the transition flow pattern, and the right end point of the platform corresponds to the transition point from the transition flow pattern to the turbulent flow pattern. When the operating gas volume increases, the gas in the gas collecting chamber below the distributor 1 can overcome the resistance and expand axially, and the effective hole area of the distributor gradually increases. Because the increase in the effective hole area will inhibit the increase in the gas and liquid velocity through the hole, the pressure of the gas and liquid can reach a dynamic balance with the resistance through the hole, so the pressure drop of the fluidized bed remains constant, and a "platform" appears on the superficial gas velocity-fluidized bed pressure drop curve.
[0052] Example 2:
[0053] For a multiphase fluidized bed system with high solid content and non-zero operating liquid volume, the method for determining the transition point of the flow pattern is the same as in Example 1, but the curves are significantly different. Figure 2 The diameter of the fluidized bed is 2.6m, and the Figure 2 The multiphase fluidized bed with porous nozzle distributor 1, solid content of 70%wt and operating liquid volume of 120t / h has a curve of superficial gas velocity and fluidized bed pressure drop as shown in Figure 4 shown. Figure 4There is no platform in the curve of superficial gas velocity-fluidized bed pressure drop. There is a section where the pressure drop increases slowly between the steep drop and the steep rise. That is, for a multiphase fluidized bed system with high solid content and non-zero operating liquid volume, the "platform" section of the superficial gas velocity-fluidized bed pressure drop curve will evolve into a "slowly rising" section. The left end point of the "slowly rising" section corresponds to the transition point from the uniform flow pattern to the transition flow pattern, and the right end point of the "slowly rising" section corresponds to the transition point from the transition flow pattern to the turbulent flow pattern. This is because the introduction of the solid phase will break the pressure balance of the fluid jet process, causing the distributor pressure drop curve to show different trends. The solid phase in the gas / liquid / solid three-phase is generally in a fluidized state in the reactor. It has some fluid properties, but its diffusivity is far worse than that of the fluid. As the distributor jet hole gradually opens, the solid phase near the side wall is continuously fluidized, and its thickness continues to decrease, causing the distributor pressure drop to continue to decrease. As the jet hole is fully opened, the solid phase thickness remains unchanged, but the gas / liquid through-hole velocity will continue to increase. Therefore, the pressure of gas and liquid and the resistance of the hole can never reach a dynamic balance, and the pressure drop of the distributor increases slowly.
[0054] Example 2
[0055] Combination Figure 5 As shown, this embodiment provides a flow pattern determination system for a multiphase fluidized bed, which is a system embodiment corresponding to the method embodiment, and can achieve the same technical effect as embodiment 1. The system includes an apparent liquid velocity acquisition module 201, an apparent gas velocity acquisition module 202, a pressure drop data acquisition module 203, and a flow pattern transition judgment module 204. Among them, the apparent liquid velocity acquisition module 201 is used to obtain the operating liquid volume data that dynamically increases from zero to the target value during the start-up phase of the multiphase fluidized bed, and convert the operating liquid volume into an apparent liquid velocity. The apparent gas velocity acquisition module 202 is used to obtain the operating gas volume data that dynamically increases from zero to the target value during the start-up phase of the multiphase fluidized bed, and convert the operating gas volume into an apparent gas velocity. The pressure drop data acquisition module 203 is used to obtain the pressure drop data corresponding to the operating liquid volume and the operating gas volume during the start-up phase of the multiphase fluidized bed. The flow pattern transition judgment module 204 is used to extract the apparent gas velocity and the pressure drop data curve of the multiphase fluidized bed under the same apparent liquid velocity, and judge the transition point between different flow patterns by the mutation point of the slope of the curve.
[0056] Example 3
[0057] The present embodiment provides a non-transient (non-volatile) computer storage medium, which stores computer executable instructions, which can execute the method in the above method embodiment 1 and achieve the same technical effect. The method includes at least the following steps: A. Obtaining the operating liquid volume data that dynamically grows from zero to the target value during the start-up phase of the multiphase fluidized bed, and converting the operating liquid volume into the apparent liquid velocity; B. Obtaining the operating gas volume data that dynamically grows from zero to the target value during the start-up phase of the multiphase fluidized bed, and converting the operating gas volume into the apparent gas velocity; C. Obtaining the pressure drop data corresponding to the operating liquid volume and the operating gas volume during the start-up phase of the multiphase fluidized bed; D. Extracting the apparent gas velocity and the pressure drop data curve of the multiphase fluidized bed at the same apparent liquid velocity, and judging the transition point between different flow types by the mutation point of the slope of the curve.
[0058] Example 4
[0059] This embodiment provides a computer program product, which includes a computer program stored on a non-transitory computer-readable storage medium, and the computer program includes program instructions. When the program instructions are executed by a computer, the computer executes the methods described in the above aspects and achieves the same technical effects.
[0060] Example 5
[0061] Figure 6 6 is a hardware structure diagram of the electronic device for determining the flow pattern of a multiphase fluidized bed in this embodiment. The device includes one or more processors 610 and a memory 620. Taking one processor 610 as an example, the device may also include: an input device 630 and an output device 640.
[0062] The processor 610 , the memory 620 , the input device 630 , and the output device 640 may be connected via a bus or in other ways.
[0063] The memory 620 is a non-transitory computer-readable storage medium that can be used to store non-transitory software programs, non-transitory computer executable programs, and modules. The processor 610 executes various functional applications and data processing of the electronic device by running the non-transitory software programs, instructions, and modules stored in the memory 620, that is, the processing method of the above method embodiment is implemented.
[0064] The memory 620 may include a program storage area and a data storage area, wherein the program storage area may store an operating system, an application required for at least one function; the data storage area may store data, etc. In addition, the memory 620 may include a high-speed random access memory, and may also include a non-transitory memory, such as at least one disk storage device, a flash memory device, or other non-transitory solid-state storage device. In some embodiments, the memory 620 may optionally include a memory remotely arranged relative to the processor 610, and these remote memories may be connected to the processing device via a network. Examples of the above-mentioned network include, but are not limited to, the Internet, an intranet, a local area network, a mobile communication network, and combinations thereof.
[0065] The input device 630 can receive input digital or character information and generate signal input. The output device 640 can include a display device such as a display screen.
[0066] The one or more modules are stored in the memory 620, and when executed by the one or more processors 610, perform: A. obtain the operating liquid volume data that dynamically increases from zero to the target value during the start-up phase of the multiphase fluidized bed, and convert the operating liquid volume into an apparent liquid velocity; B. obtain the operating gas volume data that dynamically increases from zero to the target value during the start-up phase of the multiphase fluidized bed, and convert the operating gas volume into an apparent gas velocity; C. obtain the pressure drop data corresponding to the operating liquid volume and the operating gas volume during the start-up phase of the multiphase fluidized bed; D. extract the apparent gas velocity and the pressure drop data curve of the multiphase fluidized bed at the same apparent liquid velocity, and judge the transition point between different flow types through the mutation point of the slope of the curve.
[0067] The above product can execute the method provided by the embodiment of the present invention, and has the functional modules and beneficial effects corresponding to the execution method. For technical details not described in detail in this embodiment, please refer to the methods provided by other embodiments of the present invention.
[0068] The device embodiments described above are merely illustrative, wherein the units described as separate components may or may not be physically separated, and the components shown as units may or may not be physical units, that is, they may be located in one place or distributed on multiple network units. Some or all of the modules may be selected according to actual needs to achieve the purpose of the solution of this embodiment.
[0069] Through the description of the above implementation methods, those skilled in the art can clearly understand that each implementation method can be implemented by means of software plus a general hardware platform, and of course, by hardware. Based on this understanding, the above technical solution is essentially or the part that contributes to the relevant technology can be embodied in the form of a software product, and the computer software product can be stored in a computer-readable storage medium, such as ROM / RAM, a disk, an optical disk, etc., including a number of instructions for a computer device (which can be a personal computer, a server, or a network device, etc.) to execute the methods described in each embodiment or some parts of the embodiments.
[0070] The foregoing description of specific exemplary embodiments of the present invention is for the purpose of illustration and demonstration. These descriptions are not intended to limit the present invention to the precise form disclosed, and it is clear that many changes and variations can be made based on the above teachings. The purpose of selecting and describing the exemplary embodiments is to explain the specific principles of the present invention and its practical application, so that those skilled in the art can realize and utilize various different exemplary embodiments of the present invention and various different selections and changes. Any simple modifications, equivalent changes and modifications made to the above exemplary embodiments should fall within the scope of protection of the present invention.
Claims
1. A method for determining flow pattern of a multiphase fluidized bed, characterized in that: A multiphase fluidized bed suitable for industrial scale comprises the following steps: A. Obtaining operating liquid volume data that dynamically increases from zero to a target value during the start-up phase of the multiphase fluidized bed, and converting the operating liquid volume into an apparent liquid velocity; B. obtaining operating gas volume data that increases dynamically from zero to a target value during the start-up phase of the multiphase fluidized bed, and converting the operating gas volume into superficial gas velocity; C. Obtaining pressure drop data corresponding to the operating liquid volume and the operating gas volume during the start-up phase of the multiphase fluidized bed; D. Extract the superficial gas velocity and the pressure drop data curve of the multiphase fluidized bed at the same superficial liquid velocity, and determine the transition point between different flow patterns through the mutation point of the curve slope.
2. The method for determining the flow pattern of a multiphase fluidized bed according to claim 1, characterized in that: The different flow patterns in step D are respectively a uniform flow pattern, a transitional flow pattern and a turbulent flow pattern.
3. The method for determining flow pattern of a multiphase fluidized bed according to claim 1, characterized in that: The conversion method of the apparent liquid velocity is as follows: you l =q l / r l / A; Among them, u l is the apparent liquid velocity, m / s; q l is the operating liquid volume, kg / s; ρ l is the density of the feed liquid phase, kg / m 3 , obtained from actual sampling analysis; A is the cross-sectional area of the fluidized bed reactor, m 2 .
4. The method for determining flow pattern of a multiphase fluidized bed according to claim 1, characterized in that: The conversion method of the superficial gas velocity is as follows: u g =q g / A; Among them, u g is the superficial air velocity, m / s; q g is the operating gas volume, m 3 / s; A is the cross-sectional area of the fluidized bed reactor, m 2 .
5. The method for determining flow pattern of a multiphase fluidized bed according to claim 1, characterized in that: The operating liquid volume data is 60% to 100% of the design value and is measured by the mass flow rate entering the fluidized bed.
6. The method for determining flow pattern of a multiphase fluidized bed according to claim 1, characterized in that: The operating gas volume data is adjustable according to different processes and is measured by the volume flow rate entering the fluidized bed.
7. The method for determining flow pattern of a multiphase fluidized bed according to claim 1, characterized in that: The pressure drop data is obtained by subtracting the sampled data measured by the pressure transmitters arranged at the inlet and outlet of the fluidized bed.
8. The method for determining flow pattern of a multiphase fluidized bed according to claim 1, characterized in that: The transition point between the different flow patterns is specifically a transition point from a uniform flow pattern to a transition flow pattern, or a transition point from a transition flow pattern to a turbulent flow pattern.
9. The method for determining flow pattern of a multiphase fluidized bed according to claim 1, characterized in that: The dynamic growth in step A and step B is a step-by-step growth.
10. A flow pattern determination system for a multiphase fluidized bed, characterized in that: include: An apparent liquid velocity acquisition module is used to acquire operating liquid volume data that grows dynamically from zero to a target value during the start-up phase of the multiphase fluidized bed, and convert the operating liquid volume into an apparent liquid velocity; A superficial gas velocity acquisition module, which is used to obtain the operating gas volume data that grows dynamically from zero to a target value during the start-up phase of the multiphase fluidized bed, and convert the operating gas volume into an apparent gas velocity; A pressure drop data acquisition module, which is used to acquire pressure drop data corresponding to the operating liquid volume and the operating gas volume during the start-up phase of the multiphase fluidized bed; The flow pattern transition judgment module is used to extract the superficial gas velocity and the pressure drop data curve of the multiphase fluidized bed at the same superficial liquid velocity, and judge the transition point between different flow patterns through the mutation point of the curve slope.
11. An electronic device for determining flow pattern of a multiphase fluidized bed, characterized in that: include: at least one processor; as well as a memory communicatively connected to the at least one processor; wherein, The memory stores instructions executable by the at least one processor, and the instructions are executed by the at least one processor so that the at least one processor executes the flow pattern determination method for a multiphase fluidized bed according to any one of claims 1 to 9.
12. A non-transitory computer-readable storage medium, characterized in that: The non-transitory computer-readable storage medium stores computer-executable instructions, and the computer-executable instructions are used to enable the computer to execute the flow pattern determination method for a multiphase fluidized bed according to any one of claims 1 to 9.