CN111729525A - Method for establishing liquid-liquid mixing stirring process reduced model - Google Patents
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Abstract
The invention relates to a method for establishing a reduced model of a liquid-liquid mixing and stirring process, which belongs to the technical field of chemical modeling, and comprises the following steps: screening out key mixing parameters in the liquid-liquid mixing and stirring process, then stirring a liquid-liquid mixing system in a stirring container according to the screened key mixing parameters, determining the proportion of reducing the size of a model, and obtaining the model of the liquid-liquid mixing and stirring process; the key mixing parameters in the screening liquid-liquid mixing and stirring process mainly comprise power related parameters so as to ensure the uniformity of a liquid-liquid mixing system. The method is based on the principle of geometric similarity, adopts a power-related parameter screening mode to determine the reduction proportion, and establishes a reduction model for the liquid-liquid mixing stirring process.
Description
Technical Field
The invention belongs to the technical field of chemical modeling, and particularly relates to a method for establishing a liquid-liquid mixing and stirring process reduced model.
Background
At present, liquid-liquid mixing is widely existed and is an important process link in the fields of medicines, foods, cosmetics and the like. The uniformity of liquid-liquid mixing determines the quality of the product, and therefore, the determination of the process parameters of liquid mixing and stirring becomes important for production scale. In practice, from small-scale liquid mixing during the development phase to large-scale mixing during the production phase, the parameters between the two are not linearly related, and the mixing parameters are also limited by the shape of the mixing vessel, exact identity of temperature, concentration, mass transfer and shear rate in different-scale reactors is practically impossible, and the basis of the stirring scale-up process is often on the principle of geometric similarity, and the selection of the particular dimensions of the geometric similarity is related to the mixing parameters. The mixing parameters can be the same as much as possible, and the process and the result of a small test or a pilot test can be better repeated in the industry.
The search shows that the existing model establishing method does not find the model establishment aiming at the liquid-liquid mixing and stirring process direction. As is well known, liquid-liquid mixing is widely available and is a very important process link, and for the establishment of a reduction model, it is necessary to obtain a small test or a pilot test for an earlier research and development process, so that it is very important to research the establishment method of the reduction model of the liquid-liquid mixing and stirring process.
Disclosure of Invention
Aiming at the defects in the prior art, the invention aims to provide a method for establishing a liquid-liquid mixing and stirring process reduction model, which is used for determining the reduction proportion by adopting a power-related parameter screening mode based on a geometric similarity principle and establishing the liquid-liquid mixing and stirring process reduction model.
The above object of the present invention is achieved by the following technical solutions:
a method for establishing a reduced model of a liquid-liquid mixing and stirring process, the model establishing method comprises the following steps: screening out key mixing parameters in the liquid-liquid mixing and stirring process, then stirring a liquid-liquid mixing system in a stirring container according to the screened key mixing parameters, determining the proportion of reducing the size of a model, and obtaining the model of the liquid-liquid mixing and stirring process;
the key mixing parameters in the screening liquid-liquid mixing and stirring process mainly comprise power related parameters so as to ensure the uniformity of a liquid-liquid mixing system.
By adopting the technical scheme, the reduction proportion is determined by adopting a power-related parameter screening mode based on the geometric similarity principle, and a liquid-liquid mixing stirring process reduction model is established.
The present invention in a preferred example may be further configured to: the power-related parameter is selected from one or more of actual length, actual impeller diameter, actual rotational speed, and power consumed per unit volume.
By adopting the above technical solution, wherein the above consumed power per unit volume represents the power required for stirring the liquid per unit volume. The method for mixing liquid and liquid by using constant unit volume power consumption is selected to establish the reduced model of the stirring process, so that the operation is convenient, the calculation is fast, the accuracy of the back-stepping of the reduced model is high, and the reproducibility of the test effect is good.
The present invention in a preferred example may be further configured to: the size proportion of the reduced model is less than or equal to 10.
By adopting the technical scheme, when the size proportion of the reduced model is too large (namely, when the size proportion is larger than 10), the volume of the stirring container is too small, the stirring container and the impeller of the model are difficult to manufacture, and meanwhile, if the size proportion of the reduced model is too large, the error introduced in the amplification process is large, so that the accuracy of an actual test is influenced.
The present invention in a preferred example may be further configured to: the size ratio of the reduced model is selected from 5.4-10.
By adopting the technical scheme, when the size proportion of the reduced model is too small (namely less than 5.4), the model with overlarge volume is required to be used, the volume of the reaction liquid required at the moment is relatively large, and under the condition that the size of the model with the size of more than 5.4 is selected, the size of the model can be reduced
The difference between the model and the actual production equipment is small, and the model is still suitable for being used when the size ratio is less than 5.4 under the condition of sufficient raw materials
The present invention in a preferred example may be further configured to: the material of the stirring container is selected from one or more of toughened glass, acrylic and stainless steel.
Through adopting above-mentioned technical scheme, toughened glass, ya keli, stainless steel are as stirred tank, not only are difficult to appear the condition such as rust, and long-term the use can not appear the exudate moreover, has prolonged above-mentioned stirred tank's life from this.
The present invention in a preferred example may be further configured to: the stirring container is selected from a square blending container which has no exudate after long-term use and is reduced in an equal ratio.
The present invention in a preferred example may be further configured to: the model is suitable for mixing solution with viscosity lower than 934mpa.s and volume of 0.26-1.29L; the temperature of the solution is controlled at 4-30 ℃, and the stirring time is 10-30 min.
Because the exact identity of temperature, concentration, mass transfer and shear rate in reactors of different sizes is practically impossible to the greatest extent, by adopting the above technical scheme, the modeling is carried out in an equal-scale reduction mode, at this time, more mixing parameters can be the same as much as possible, at this time, the process of pilot plant test or pilot plant test can be better repeated in the industry, and the result is obtained.
The present invention in a preferred example may be further configured to: in the model establishing method, the rotating speed of the model is calculated according to the actual rotating speed, and the conversion formula is as follows:
N2＝N1(D1/D2)2/3；
wherein N is1Is the actual rotational speed, N2Is the rotational speed of the model, D1To the actual impeller diameter, D2Is the impeller diameter of the model.
By adopting the technical scheme, the rotating speed of the model is only related to power related parameters such as the actual rotating speed, the actual impeller diameter and the impeller diameter of the model, so that the diameter of the stirring impeller is calculated in the actual model manufacturing process.
The invention also discloses a model established by adopting the liquid-liquid mixing and stirring process reduction model establishing method.
In conclusion, the invention has the following beneficial effects:
1. the method is based on the principle of geometric similarity, adopts a power-related parameter screening mode to determine the reduction proportion, and establishes a reduction model for the liquid-liquid mixing stirring process.
2. When the size proportion of the reduced model is too large (namely, when the size proportion is more than 10), the volume of the stirring container which needs to be adopted is too small, the stirring container and the impeller of the model are difficult to manufacture, and meanwhile, if the size proportion of the reduced model is too large, the error introduced in the amplification process is large, and the accuracy of an actual test is further influenced.
Drawings
Fig. 1 is a graph of the mixing effect of mixing and stirring for 0min, 3min, 10min and 20min in the liquid-liquid mixing test after reduction in application example 1 of the present application, and is mainly used for embodying the mixing condition of the glycerol solution of methylene blue in the glycerol solution.
Detailed Description
The present invention will be described in further detail with reference to examples.
First, an embodiment
Example 1: a method for establishing a reduced model of a liquid-liquid mixing and stirring process comprises the following specific steps:
(1) and (3) determining the size proportion of the reduced model: the size of the geometric similarity model depends on the scaling factor L2/L1When L is present2/L1At 10 or more, the error introduced by the enlargement process is large, and therefore the size of the model should be larger than 1/10 for the actual use of the agitation vessel. In general, L is preferred2/L1The model was constructed with a scale of 5.4 as an example.
(2) Abbreviations and definitions:
L2is the actual length;
L1is the length of the model;
N1is the actual rotational speed;
N2is the rotational speed of the model;
D1actual impeller diameter;
D2is the impeller diameter of the model.
(3) Conversion of stirring speed:
the power consumed per unit volume represents the power required to stir each unit volume of liquid. Therefore, the stirring process is amplified from research and development to production scale according to the consumed power per unit volume, so that the consumption of the step-by-step amplification experiment is reduced.
In the experiment, the main device for stirring is the impeller, and the stirring of the impeller can drive the liquid in the stirring container to move, so that the stirring power P is adopted in the experiment to replace the unit volume consumed power for carrying out experimental calculation.
The stirring power P is ρ gQH,
wherein rho is the density of the liquid, g is the acceleration of gravity, Q is the liquid discharge capacity of the impeller, and H is the energy transferred to the liquid by the impeller.
Liquid discharge quantity Q of impeller is equal to NQNd3，
Wherein N isQThe number of the circulating flow, N the rotating speed and d the diameter of the impeller.
Energy H-u transferred to unit weight of liquid by impeller2/2g，
Wherein u is the speed of the liquid leaving the impeller and g is the acceleration of gravity.
Due to u2Is proportional to N2d2H is thus proportional to N2d2The stirring power P is proportional to the third power of the rotation speed and the fifth power of the stirring diameter, i.e. P-3D5。
For a fixed stirred vessel, the size of the stirred vessel is a multiple of the diameter of the impeller, such that the volume of the stirrer is proportional to the cube of the impeller diameter, i.e., the ratio of the length, width and height of the vessel before and after amplification, i.e., V ═ D · H, i.e., V · D ·3。
And (3) dividing the two formulas to obtain:
P/V∝N3D2；
this is the stirring power consumed per unit volume. To keep P/V unchanged, there is N1 3D1 2＝N2 3D2 2；
That is, (N)2/N1)3＝(D1/D2)2；
I.e. the rotational speed N of the model2＝N1(D1/D2)2/3；
Wherein P is the stirring power; n is the rotating speed; d is the stirring diameter; v is the agitator volume.
Converting a formula:
N2＝N1(D1/D2)2/3；
therefore, the conversion of the stirring speed is only related to the stirring impeller, and therefore, in the actual modeling process, the calculation should be performed based on the size of the stirring impeller.
Second, application example
(I) establishment of model size in actual production stage reduced to research and development stage
Application example 1: a liquid-liquid mixing and stirring process reduces the model, the actual production uses Sartorius Stedim to provide a disposable magnetic stirring and mixing system (Sartorius Stedim recommends that its stirring bag use minimum 20% of full load), is 200L square stirring bag (length, width, height 617, 525mm), and the stirring bag is internally provided with four-blade magnetic stirring paddle with a circular base, the overall length is 161mm, and the blades are 58mm squares, and are symmetrically embedded on the circular base.
(1) Under the actual production conditions
At the temperature of 25 ℃, 20L of glycerol is poured into a disposable magnetic stirring and mixing system, 400ml of methylene blue glycerol solution (namely methylene blue dyed glycerol) is added, and the mixture is mixed and stirred for 20min at the speed of 160rpm, and the mixed solution has no color difference and better uniformity through detection.
The actual dimensions are: length, width, height 617, and 525 mm;
as can be seen from table 1, the dimensions of the die were 115.0 × 97.8mm in length and width, and the scale up was 5.4.
In this modeling process, N2＝N1(D1/D2)2/3＝N1(30/161)2/3＝0.3262N1。
(2) As can be seen from the liquid-liquid mixing test after the reduction,
at 25 deg.C, 1L of glycerol was poured into a mold container, 20ml of methylene blue glycerol solution (i.e., methylene blue-stained glycerol) was added, and the mixture was stirred at 496rpm for 20min using an IKA cantilever stirrer (MICROSCAR 15CONTROL) and a custom impeller having a total length of 3cm, and the mixing effects of 0min, 3min, 10min and 20min were recorded as shown in FIG. 1.
As can be seen from FIG. 1, under the stirring speed of 496rpm, the mixing effect of the glycerol solution of methylene blue and glycerol after stirring for 3min is poor, the glycerol solution of methylene blue is not diffused yet, and the liquid-liquid mixed solution has obvious color difference; when the solution is stirred for 10min, a certain color difference still exists at the local part of the liquid-liquid mixed solution; when the stirring time is 20min, the color difference is not obvious, and the uniformity is better.
The model has the phenomena of uneven mixing or overlong mixing time (namely the mixing time is more than 1 hour) and the like when the liquid with higher viscosity is stirred, and the viscosity of glycerol is 934mPa.s at the temperature of 25 ℃, so that the model is suitable for mixing the liquid with the viscosity of less than 934 mPa.s.
Application examples 2 to 8: a liquid-liquid mixing stirring process shrinkage model is different from application example 1 in that: the scale of reduction varies and the size of reduction to the development stage that can be calculated is shown in table 1 below.
TABLE 1
In the actual operation process, L needs to be selected2/L1Model less than 10, when defining L2/L1When the volume is larger than 10, the use volume of the model is too small, and the test error is larger. When L is2/L1When the volume is less than 3.6, a model with an excessive volume needs to be used, and the volume of the stock solution needs to be large. Considering comprehensively, select L in application example 12/L1The model was constructed with a scale of 5.4 as an example.
The dimensions of the die were length, width, height, 115.0, 97.8mm, the scale being 5.4.
In this modeling process, N2＝N1(D1/D2)2/3＝N1(30/161)2/3＝0.3262N1。
The rotational speed is therefore comparable to table 2 below.
TABLE 2
In the pilot test building stage, when the pilot test stage is reduced to the size of a model in the development stage, Sartorius Stedim is used for providing a disposable magnetic stirring and mixing system, the system is a 100L square stirring bag (length, width, height, 496 and 406mm), a circular base and four-blade magnetic stirring paddle are arranged in the stirring bag, and the overall length is 161 mm.
Application example 9: a liquid-liquid mixing stirring process shrinkage model is different from application example 8 in that: the reduction scale is the same as the impeller diameter of the model, but the size of the reduced model container is different, and the volume of the model is different.
Application example 10: a liquid-liquid mixing and stirring process reduction model is different from the application example 7 in that: the reduction scale is the same as the impeller diameter of the model, but the size of the reduced model container is different, and the volume of the model is different.
Application example 11: a liquid-liquid mixing stirring process reduction model is different from the application example 6 in that: the reduction scale is the same as the impeller diameter of the model, but the size of the reduced model container is different, and the volume of the model is different.
Application example 12: a liquid-liquid mixing stirring process shrinkage model is different from application example 5 in that: the reduction scale is the same as the impeller diameter of the model, but the size of the reduced model container is different, and the volume of the model is different.
Application example 13: a liquid-liquid mixing stirring process shrinkage model is different from application example 1 in that: the reduction scale is the same as the impeller diameter of the model, but the size of the reduced model container is different, and the volume of the model is different.
Application example 14: a liquid-liquid mixing stirring process shrinkage model is different from application example 2 in that: the reduction scale is the same as the impeller diameter of the model, but the size of the reduced model container is different, and the volume of the model is different.
Application example 15: a liquid-liquid mixing stirring process reduction model is different from the application example 3 in that: the reduction scale is the same as the impeller diameter of the model, but the size of the reduced model container is different, and the volume of the model is different.
Application example 16: a liquid-liquid mixing stirring process reduction model is different from the application example 4 in that: the reduction scale is the same as the impeller diameter of the model, but the size of the reduced model container is different, and the volume of the model is different.
Data for applications 9-16 as can be seen in table 3,
TABLE 3
As can be seen from the test data in tables 1 and 3, L is selected in the actual operation process by comparing the control variables with different reduced model container sizes and different reduction ratios2/L1Model less than 10, when defining L2/L1When the volume is larger than 10, the use volume of the model is too small, and the test error is larger. When L is2/L1Less than 3.6, the use of a model with an excessively large volume is required, and therefore the use of the reduced scale in application examples 11 to 16 is recommended. Meanwhile, in the scheme, the impeller sizes of the stirring bags with the specifications of 100L and 200L are the same, so that the selected L is selected2/L1The model was constructed with a scale of 5.4 as an example.
In this modeling process, N2＝N1(D1/D2)2/3＝N1(30/161)2/3＝0.3262N1。
The rotational speed is therefore comparable to table 4 below.
TABLE 4
Application example 17: a method for establishing a liquid-liquid mixing stirring process reduced model is different from application example 1 in that: the type of solution and viscosity used are different.
The operation steps comprise: an acetic acid-sodium acetate buffer solution having a pH of 5.0 was prepared after mixing a 5% sodium hydroxide solution having a viscosity of 1.075mpa.s at 30 ℃ and acetic acid having a viscosity of 1.040mpa.s at 30 ℃ and then stirring at a stirring speed of 92r/min for 20min at a temperature of 30 ℃ using an IKA stirrer (model: MICROSTAR 15 CONTROL). And the pH detection is carried out on 3 different positions of the container, and the detected pH is 5.0 +/-0.3. From this, it was found that the above acetic acid-sodium acetate buffer solution was stirred for 20min and then the solution was homogeneous.
Thirdly, the proportion of the stirring impeller is reduced
Original size: the four-blade stirring paddle with the circular base is a square with the overall length of 161mm and 58 x 58mm blades, and is symmetrically embedded in the circular base.
The total length required after shrinking is 3 cm: square paddle: 1.08 × 1.08 cm; four square blades are symmetrically distributed on the base; the diameter of the circular base is 1.7 cm.
Fourthly, requirements for making model
The requirements of stirring equipment are as follows: the shear force of the stirring bag used in the actual production, which is researched by Sartorius Stedim, shows that the optimal rotating speed range of the stirring bag is 28-110rpm, so that the stirring device used in the model can accurately control the speed within the range of 85-338 rpm.
Stirring a container: should be for the square mixing system of geometric proportion minification, long-term use does not have the exudate, through to multiple material contrast, the material can be preferably toughened glass, ya keli, stainless steel etc.. The size of the model is 115mm x 115mm, the actual manufacturing height is higher than 98mm, the size of the model for pilot plant is 92.4mm x 92.4mm, and the actual manufacturing height is higher than 75.5 mm.
The specific embodiments are only for explaining the present invention, and the present invention is not limited thereto, and those skilled in the art can make modifications without inventive contribution to the present embodiments as needed after reading the present specification, but all of them are protected by patent law within the scope of the claims of the present invention.
Claims (9)
1. A method for establishing a reduced model of a liquid-liquid mixing and stirring process is characterized by comprising the following steps: screening out key mixing parameters in the liquid-liquid mixing and stirring process, then stirring a liquid-liquid mixing system in a stirring container according to the screened key mixing parameters, determining the proportion of reducing the size of a model, and obtaining the model of the liquid-liquid mixing and stirring process;
the key mixing parameters in the screening liquid-liquid mixing and stirring process mainly comprise power related parameters so as to ensure the uniformity of a liquid-liquid mixing system.
2. The method for building a liquid-liquid mixing and stirring process reduction model according to claim 1, wherein the power-related parameter is selected from one or more of actual length, actual impeller diameter, actual rotating speed and consumed power per unit volume.
3. The method for establishing the shrinkage model of the liquid-liquid mixing and stirring process according to claim 1, wherein the size ratio of the shrinkage model is less than or equal to 10.
4. The method for building a scaled model of a liquid-liquid mixing and stirring process as claimed in claim 3, wherein the scaled model is selected from a range of 5.4 to 10.
5. The method for establishing the liquid-liquid mixing and stirring process shrinkage model according to claim 1, wherein the stirring container is made of one or more materials selected from tempered glass, acrylic and stainless steel.
6. The method for establishing a scaled model of a liquid-liquid mixing and stirring process according to claim 1, wherein the stirring vessel is selected from a group of blending vessels that have no exudate after long-term use and are scaled down in an equal proportion.
7. The method for establishing the liquid-liquid mixing and stirring process shrinkage model according to claim 1, wherein the model is suitable for mixing a solution with the viscosity of less than 934mpa.s and the volume of 0.26-1.29L; the temperature of the solution is controlled at 4-30 ℃, and the stirring time is 10-30 min.
8. The method for establishing the reduced model of the liquid-liquid mixing and stirring process according to any one of claims 2 to 7, wherein in the method for establishing the model, the rotating speed of the model is calculated according to the actual rotating speed, and the conversion formula is as follows:
N2=N1(D1/D2)2/3；
wherein N is1Is the actual rotational speed, N2Is the rotational speed of the model, D1To the actual impeller diameter, D2Is the impeller diameter of the model.
9. A model established by the liquid-liquid mixing stirring process reduction model establishing method according to any one of claims 1 to 7.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114822758A (en) * | 2022-06-28 | 2022-07-29 | 新泰市中医医院 | Automatic mixing control method and system for liquid medicine in endocrinology department |
| CN116943464A (en) * | 2023-08-03 | 2023-10-27 | 广州芙莉莱化妆品有限公司 | Cosmetic stirring parameter conversion method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20110116342A1 (en) * | 2009-05-11 | 2011-05-19 | Millipore Corporation | Method for scaling mixing operations |
| CN107561938A (en) * | 2017-08-30 | 2018-01-09 | 南京大学 | Micro-interface enhanced reactor reaction rate structure imitates regulation-control model modeling method |
| CN108504548A (en) * | 2018-04-03 | 2018-09-07 | 农业部规划设计研究院 | A kind of design optimization method of full-mixing type anaerobic fermentation reactor |
| CN210079321U (en) * | 2019-03-27 | 2020-02-18 | 常熟恩赛生物科技有限公司 | Liquid-liquid mixing PE tank |
-
2020
- 2020-06-24 CN CN202010586060.1A patent/CN111729525A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20110116342A1 (en) * | 2009-05-11 | 2011-05-19 | Millipore Corporation | Method for scaling mixing operations |
| CN107561938A (en) * | 2017-08-30 | 2018-01-09 | 南京大学 | Micro-interface enhanced reactor reaction rate structure imitates regulation-control model modeling method |
| CN108504548A (en) * | 2018-04-03 | 2018-09-07 | 农业部规划设计研究院 | A kind of design optimization method of full-mixing type anaerobic fermentation reactor |
| CN210079321U (en) * | 2019-03-27 | 2020-02-18 | 常熟恩赛生物科技有限公司 | Liquid-liquid mixing PE tank |
Non-Patent Citations (2)
| Title |
|---|
| 张鹏: "XJM-S型浮选机相似放大方法研究", 《洁净煤技术》 * |
| 袁松范: "搅拌混合设备及其放大", 《医药工程设计》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114822758A (en) * | 2022-06-28 | 2022-07-29 | 新泰市中医医院 | Automatic mixing control method and system for liquid medicine in endocrinology department |
| CN114822758B (en) * | 2022-06-28 | 2022-09-09 | 新泰市中医医院 | Automatic mixing control method and system for liquid medicine in endocrinology department |
| CN116943464A (en) * | 2023-08-03 | 2023-10-27 | 广州芙莉莱化妆品有限公司 | Cosmetic stirring parameter conversion method |
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