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Modeling method for mass transfer rate structure-effect regulating model of micro-interface enhanced reactor

A model modeling and reactor technology, applied in the fields of instruments, special data processing applications, chemical process analysis/design, etc., can solve the problems of difficult universal application, high energy consumption and high manufacturing cost of microbubble equipment

Active Publication Date: 2017-11-14
NANJING UNIV
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

In addition, the energy consumption and manufacturing cost of the equipment for generating microbubbles are too high
[0007] (2) There are no micro-bubble system characteristics based on the continuous liquid phase and high turbulence at home and abroad. Systematic micro-interface mass transfer enhancement theory, micro-bubble testing and characterization methods, and micro-interface enhanced reactor structure-effect control theory have not been proposed. and related mathematical models
There are many such models, and their drawbacks are: the obtained correlations are obtained under specific conditions (including specific reactor structures, stirring methods, gas-liquid physical properties, operating conditions, measurement methods, etc.), which are difficult to apply universally
However, for the micro-interface strengthening reactor, the work in this area is still blank in the world.

Method used

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  • Modeling method for mass transfer rate structure-effect regulating model of micro-interface enhanced reactor
  • Modeling method for mass transfer rate structure-effect regulating model of micro-interface enhanced reactor
  • Modeling method for mass transfer rate structure-effect regulating model of micro-interface enhanced reactor

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Experimental program
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Embodiment 1

[0273] Method of the present invention specifically comprises the steps:

[0274] Step 10: Establish the gas side mass transfer coefficient k G Computational model;

[0275] According to membrane theory, the gas side mass transfer coefficient k G The size is determined by the gas phase diffusion coefficient D G and effective gas film thickness δ G Decide;

[0276] Based on the Chapman-Enskog motion theory, D G The general form of is:

[0277]

[0278] In the formula, T is the gas temperature; M A , M B Respectively, the molar mass of gas A and solvent B, Kg / mol; P G is the average pressure of the gas in the bubbles in the reactor, Pa;

[0279] For medium and high temperature gases, the accuracy of the above formula is relatively high, and the general error is within 5-10%. It can be seen from the formula that when the gas composition is constant, D G It increases with the increase of temperature and decreases with the increase of gas partial pressure. D of low d...

Embodiment 2

[0461] This embodiment takes figure 1 The reactor shown is taken as an example to illustrate the application of the model constructed by the modeling method described in Example 1 in the carbon dioxide and water system reactor. figure 1 The structure of the reactor can be the structure of the existing reactor, and only the method of the present invention is used for parameter design, and the structure of the reactor is not described in detail in the present invention.

[0462] The mass transfer rate structure-effect control model constructed according to Example 1 is as follows:

[0463]

[0464]

[0465]

[0466] d min =11.4(μ L / ρ L ) 0.75 ε -0.25 (33)

[0467] d max =0.75(σ L / ρ L ) 0.6 ε -0.4 (36)

[0468]

[0469]

[0470]

[0471]

[0472]

[0473]

[0474]

[0475]

[0476]

[0477] In the formula, d 32 is the average Sauter diameter of bubbles in the reactor, m; d min 、d max are the largest and smallest bubble diamet...

Embodiment 3

[0478] The model selected in embodiment 3 mainly considers L mix less than L b The situation, because the opposite situation is not common, more extreme. The structural parameters of the reactor also need to satisfy: λ 1 =0.1~0.5、K 1 =0.5,L b =13D 1 .

[0479] For carbon dioxide and water system, when the operating conditions are: Q L =2000L / h(5.56×10 -4 m 3 / s), gas flow Q G =0.2Q L , T=298K, P G0 =1atm; and the physical parameters of the liquid phase in this system are: ρ L =1000kg / m 3 , μ L =8.9×10 -4 Pa s, σ L =7.197×10 -4 N / m; diameter of reactor bubble breaker tube D 1 =0.02m; E 0 Indicates the energy input by the system, that is, the rated power on the nameplate of the circulating pump, take E 0 = 1000W. According to the operating conditions and the above model, the average diameter of bubble Sauter is calculated by applying MIR 32 The mass transfer rates of gas side and liquid side when =0.1mm are k G =1.78×10 -6 mol / Pa·m 3 s, k L =5.75×10 -4 ...

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Abstract

The invention discloses a modeling method for a mass transfer rate structure-effect regulating model of a micro-interface enhanced reactor. Rigorous theoretical derivation is adopted for respectively establishing a gas-side mass transfer coefficient calculation model and a liquid-side mass transfer coefficient calculation model. The mass transfer rate structure-effect regulating model established according to the modeling method disclosed by the invention can be adopted for directly viewing the relationship between the mass transfer rate and the bubble size and a theoretical basis is established for researching a micro-interface system, so that the target of acquiring the maximum energy efficiency and physical effect in the reaction process can be achieved in the manner of regulating structure parameter and operation parameter or an efficient reactor structure is designed under the conditions of given reaction target (task), energy consumption and material consumption.

Description

technical field [0001] The invention belongs to the technical fields of chemical manufacturing, reactors and modeling, and in particular relates to a modeling method for a structure-effect control model of a micro-interface enhanced reactor mass transfer rate. Background technique [0002] Heterogeneous reactions such as oxidation, hydrogenation, and chlorination widely exist in chemical production processes, and their macroscopic reaction rates are generally restricted by mass transfer processes. The mass transfer rate of the gas-liquid reaction is mainly affected by the liquid side (or gas side) mass transfer coefficient and the gas-liquid interfacial area a. Previous studies have shown that a has a greater influence on the volumetric mass transfer coefficient and is easy to control. Therefore, increasing a is considered to be a particularly effective way to improve the reaction efficiency of gas-liquid reaction systems controlled by mass transfer. [0003] Bubble Sauter...

Claims

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Application Information

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IPC IPC(8): G06F19/00
CPCG16C20/10
Inventor 张志炳田洪舟周政张锋李磊王丹亮李夏冰
Owner NANJING UNIV
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