Stirrer Type Research Articles

ОПТИМИЗАЦИЯ РЕЖИМА 3-D ПЕЧАТИ ТУРБИННОЙ МЕШАЛКИ ДЛЯ ДИСПЕРГИРОВАНИЯ РАСТВОРОВ ПОЛИМЕРНЫХ КОМПОЗИТОВ

The design of the turbine stirrer is characterized by a rather complex shape of working surfaces and during its manufacture by traditional methods unique molds are required for each type of stirrer, increased material and labor costs are required. The use of 3D printing allows you to obtain products with a complex surface configuration, with minimal costs and which do not require subsequent machining. Analysis was carried out and selection of 3D printing type and material of turbine stirrer intended for mixing of elastomeric nanocomposite solutions components was carried out. FDM (Fused Deposition Modeling) is the most suitable type of 3D printing for solving design and technological problems in the manufacture of turbine stirrers. Plastics of the brands ABS, PLA and PETG have become very widespread in this type of 3D printing. The highest mechanical properties, chemical resistance and the lowest price of the materials under consideration are PETG plastic, which was chosen for the manufacture of a turbine stirrer designed to mix and disperse solutions of elastomeric nanocomposites. An active experiment was implemented according to the В2 plan. The samples are PETG plastic plates printed on a Flying Bear Ghost 5 3D printer. The main mode parameters of 3D printing by FDM type, which determine the strength of samples and printing performance, are: the number of concentric lines that make up the wall of the printed product and the line width. A regression model of the dependence of strength of samples made of PETG plastic on the number and width of lines in 3D printing was obtained. The optimal 3D printing mode of the turbine stirrer is set, providing high strength of the product and performance of the technology.

Призначення, модифікації і експлуатація резервуарного обладнання хімічних цехів коксохімічних виробництв

DOI: 10.31081/1681-309X-2024-0-2-48-56 Specialty 161. U.D.C. 662.74.001.24(07) PURPOSE, MODIFICATION AND OPERATION OF CAPACITIVE EQUIPMENT OF BY-PRODUCT PLANTS OF COKE PRODUCTION © Ye.I. Kudriavtsev, L.O. Kazak (STATE ENTERPRISE "STATE INSTITUTE FOR DESIGNING ENTERPRISES OF COKE OVEN AND BY-PRODUCT PLANTS'' (SE "GIPROKOKS''), 61002, 60 Sumska str., Kharkiv, Ukraine) The article presents an overview of capacitive equipment used in chemical shops of coke production. The advantages of metal modern capacitive equipment and the possibility of its long-term operation in present conditions are analysed. The basic principles are highlighted of selection when designing the type and materials of tanks and related equipment, which include heating devices, pumping equipment, various types of stirrers, coils, level, pressure and temperature measuring devices, breathing, hydraulic, safety and emergency valves, etc. In particular, the volume, material, wall thickness, and design of the bottoms and roofs of capacitive equipment depends not only on the technological features of the designed process in which it is used, but also on such factors as seismicity of the installation area, natural conditions, available industrial sites, etc. Information on modern requirements for the design features of capacitive flow-through equipment is provided, and the advantages of various design features are highlighted. The most modern and progressive features of the materials used, the principles of designing tank heating systems, etc. are presented. A generalised classification scheme for capacitive equipment is provided. The main requirements for modern capacitive equipment for various technological purposes are formulated: reliability and structural strength, due to the choice of technical solutions and materials resistant to the effects of product components present in this equipment. Examples of designed and installed equipment using different types of steel are given. Brief information is provided on the latest developments of SE “GIPROKOKS” that are of interest for use in coke production, taking into account the positive experience of operation, originality and efficiency of technical solutions, and specific features of particular enterprises. Keywords: coke production, design, capacitive equipment, tank, collector, heater, mechanised illuminator, material, heating, operation. Corresponding author Ye.I. Kudriavtsev, e-mail: jonnykvn1979@gmail.com

Structural improvement of propeller impellers of high-temperature and high-pressure reactor based on TRIZ theory

With the rapid development of science and technology, exploration and study of extreme environments have advanced significantly. Consequently, the demand for equipment designed to operate under these conditions has increased. This paper proposes an innovative design method for stirring impeller structures based on the Teoriya Resheniya Izobreatatelskikh Zadatch (TRIZ) theory. By analyzing the interaction between components during the stirring process, we establish a TRIZ conflict resolution-based model for the innovative design process of stirring impeller structures. Our innovative design process is model-led, based on the TRIZ conflict resolution theory. This process improves existing stirrer structures to design a new type of stirrer with an ultra-thin multi-cross-shaped hole structure. We compare our proposed structural model to an existing stirrer using Computational Fluid Dynamics (CFD) for numerical simulation. The effect of different thicknesses, numbers of holes, radii, and shapes of the frame stirrer on the flow field values was analyzed. The results indicate that reducing the stirrer thickness, increasing the number of holes, and perforating the stirring impeller can enhance its stirring capacity. Changing the opening radius and adding special-shaped holes to the stirring impeller can also modify its stirring capacity. Ultimately, the proposed frame stirrer with an ultra-thin multi-cross-shaped hole structure increases the maximum turbulence kinetic energy by 14.6% and the maximum speed by 32.9% compared to the existing stirrer. Studying the feasibility of this innovative model and design method can provide new ideas for designing high-temperature and high-pressure reactor impellers in extreme environments.

Fragmentation of Aspergillus niger pellets in stirred tank bioreactors due to hydrodynamic stress

Filamentous fungi are widely exploited as cell-factories in industry due to their metabolic diversity, high production capacity and secretion efficiency. In stirred tank bioreactors, the filamentous fungus Aspergillus niger builds agglomerates of complex morphology. The formed morphology has a decisive influence on productivity and is significantly influenced by the hydrodynamic stress induced by the stirrer. Due to the complex interactions between the cultivation parameters, an examination solely of the influence of the stirrer is difficult. In this work, fragmentation experiments were established and conducted allowing the selective examination of the impact of stirrer type and stirring intensity on the bio-agglomerates’ morphology at a reasonable effort. With the applied method, a clear order of stress intensity for different stirrer types was found. Studying the breakage mechanism, both fracture and abrasion have been found to occur, significantly depending on the employed stirrer type. The impeller swept volume model has been proven to correlate the particle size well for the employed stirrer types. In the literature, most work on the characterisation of stirrer types concerning hydrodynamic stress has been done using model systems. The extensive results obtained earlier at our department using a liquid/liquid model system agree with the results of this work.

A new method for determining protein solubility index (PSI) based on extraction with 5 mM alkali hydroxide and its correlation with trypsin inhibitor activity in soybean products

AbstractProtein quality affects the nutritional values and functional properties of protein products. For better utilization, it is important to assess protein quality accurately and cost‐effectively. For decades, several indirect indices have been relied on, including nitrogen solubility index, protein dispersibility index, urease activity, and protein solubility in 0.2% potassium hydroxide. However, each existing index has limitations or practical difficulties for measurement, while different procedures and terminologies often cause confusion. For rectifying this situation, a new protein quality index, the protein solubility index (PSI), was developed. This required investigation of many factors, including alkali hydroxide type and concentration, solid to solvent ratio, extraction time, magnetic stirring speed, magnetic stirrer type, and centrifugation force and time. For nitrogen analysis, a combustion method was used, where effects of using extracts or residues, sample moisture, sample mass, and the sequence of drying and weighing residues were also investigated. The new PSI method employs 5 mM alkali hydroxide extraction, magnetic stirring, nitrogen analysis of dried residues and small sample size. It allows simultaneous running of multiple samples. Furthermore, the correlations between trypsin inhibitor activity (TIA) and PSI were either strong or very strong (r = 0.747**–0.974**), depending on sample sets. The 5 mM extraction procedure produced a stronger correlation between protein extractability and TIA than the extraction procedure for the TIA assay (10 mM NaOH, 3 h). PSI has a potential to replace most, if not all, of the indirect indices for protein quality of various products, providing a unified index for relevant industries.

Influence of different stirring setups on mass transport, gas hydrate formation, and scale transfer concepts for technical gas hydrate applications

AbstractThis contribution describes the influence of turbulent flow conditions in the liquid and/or gas phase and directly in the phase interface, different flow patterns (axial/radial), volume‐specific power inputs, mass‐specific energy consumptions, as well as volume‐specific mass transfer coefficients on the gas hydrate formation, derived from an experimental investigation of five different reactor setups. The results correspond to all fields of gas hydrate research, especially actually discussed technical hydrate applications, like hydrate‐based desalination, gas storage, gas separation, biogas and green hydrogen handling, carbon dioxide deposition, new phase transfer materials, and even electrical power supply. Two main objectives, first, to determine favorable hydrate forming conditions in stirred systems to provide competitive hydrate formation processes, and second, the search for a concept to enable the transfer of experimental results, for example, from a stirred reactor to a pipeline system for inhibitor research, through the targeted adjustment of similar and comparable turbulent flow conditions in different reactor setups could be achieved. So far, the targeted formation of gas hydrates has been investigated essentially from the point of view of optimizing the formation conditions with regard to pressure and temperature as well as the addition of auxiliary materials and promoters. In addition, some studies consider different reactor types and setups, for example, spray reactors or bubble columns. In many publications, stirred and cooled pressure autoclaves are described, whereby the gas and the liquid phase are brought into contact with each other by mixing to a greater or lesser extent by an agitator, then forming a solid gas hydrate phase. Often missing in previous research work is a systematic approach for determining the influence of flow conditions on gas hydrate formation. Many different influencing factors in a stirred reactor system can strongly affect the kinetics and formation of gas hydrates, for example, stirrer type, rotational frequency, stirrer and reactor geometry, and filling level. This is the starting point of the present investigation that deals with the influence of the flow conditions on the formation of gas hydrates. Tests were performed in a stirred autoclave to measure the effects of different stirrer configurations. The results obtained contribute to the explanation of the hydrate formation mechanism and can be used to optimize the targeted production of gas hydrates in technical hydrate applications. A rapid, immediate, hydrate formation is advantageous and can be achieved by suitable flow conditions in stirred reactors, which is successfully proven within this study contribution.

Characterization of a small-scale crystallizer using CFD simulations and X-ray CT measurements

• Single and multiphase CFD of a small-scale crystallizer with two stirrer types. • Indications when each stirrer is preferably used based on hydrodynamics. • X-ray CT applied in mixing studies used for the validation of the CFD simulations. Although small-scale crystallizers have gained increasing importance in recent years, their hydrodynamic properties have not yet been thoroughly studied. The purpose of this work is to characterize an intensively stirred small-scale crystallizer and to analyze whether its fluid mechanics behavior deviates from being homogeneously well-mixed. To this aim, single and multiphase computational fluid dynamics (CFD) simulations have been conducted. Two types of stirrers, including one overhead stirrer (OS) and one magnetic stirrer (MS), were compared. The single-phase CFD simulations showed that the mixing characteristics of the two stirrers differ significantly, thereby leading to variations in the distribution of solids. The MS is an axial flow type impeller, which is better at handling solid suspensions than the OS. The simulations were complemented by X-ray computed tomography measurements, which confirmed that spatial variations in solid distribution occur and that assuming a homogeneous suspension might lead to errors when modeling crystallization processes.

Large-Scale Production of Size-Adjusted β-Cell Spheroids in a Fully Controlled Stirred-Tank Reactor

For β-cell replacement therapies, one challenge is the manufacturing of enough β-cells (Edmonton protocol for islet transplantation requires 0.5–1 × 106 islet equivalents). To maintain their functionality, β-cells should be manufactured as 3D constructs, known as spheroids. In this study, we investigated whether β-cell spheroid manufacturing can be addressed by a stirred-tank bioreactor (STR) process. STRs are fully controlled bioreactor systems, which allow the establishment of robust, larger-scale manufacturing processes. Using the INS-1 β-cell line as a model for process development, we investigated the dynamic agglomeration of β-cells to determine minimal seeding densities, spheroid strength, and the influence of turbulent shear stress. We established a correlation to exploit shear forces within the turbulent flow regime, in order to generate spheroids of a defined size, and to predict the spheroid size in an STR by using the determined spheroid strength. Finally, we transferred the dynamic agglomeration process from shaking flasks to a fully controlled and monitored STR, and tested the influence of three different stirrer types on spheroid formation. We achieved the shear stress-guided production of up to 22 × 106 ± 2 × 106 viable and functional β-cell spheroids per liter of culture medium, which is sufficient for β-cell therapy applications.

Role of Iron-Rich Phases and Porosity on the Ductility of Rheocast Al-Mg-Si-Alloys

Treatment of the slurry is important during RheoMetalTM casting. In this work, semi-solid slurries were prepared under different stirring intensities, using two types of stirrers: a naked rod (for regular stirring) and a rod with two blades (for intensified stir). Tensile tests were performed, investigating fracture surfaces, as well as metallographic samples. The results show that intensified stir produces castings with finer primary particles and a more homogeneous microstructure. On the other hand, more faceted Fe-rich phases are found along the α-Al grains boundary as well, due to the dissolution of Fe from the stirrers. Moreover, for intensified stir castings, the porosity found on the fracture surfaces are smaller, while more brittle eutectic phases and second (intermetallic) phases, especially Fe-rich phases, are observed. Consequently, the castings with intensified stir show worse ductility. Finally, a quantitative analysis was made regarding ductility, affected both by porosity and the presence of Fe-rich phases.

Heat exchange in a chamber apparatus with a circulation circuit during cheese masses production

Chamber heat exchangers are used in various branches of the food industry. Different types of stirrers are used in them as the means of intensifying heat transfer. They also give the devices the function of mixing devices. Grinding mechanisms are installed in some designs, which also affect the heat transfer and hydrodynamics of the movement. Grinding and mixing devices are especially widely used in the production of composite products. During heat treatment, uniformity of heating of the whole mass and the same duration of action of the maximum temperature is important for many products. In such cases, it is advisable to use chamber heat exchangers with a circulating circuit for processing thermolabile products. The heat exchange in such a device is complex due to the hydrodynamics of the product. Studies of the heat exchange process in a capacitive device with a circulating circuit are relevant. In particular, the establishment of the criterion equation of heat transfer to determine the heat transfer coefficient from the wall of the device to the product. The article deals with the peculiarities of heat exchange when using chamber heat exchangers with a stirrer and a circulating circuit. The results of research on the heat exchange process at the production of composite products on the basis of cottage cheese are presented. The process of heating the mass is influenced by its movement through the circulating device and in a closed circuit. Therefore, to study the effect of purely mechanical treatment on the heating process of the product, we studied the change in the temperature of the mass at the outlet of the circulation circuit without the supply of a heating agent. According to the results of the research, it was found that the circulation of the product in a closed circuit allows ensuring uniform heating and reduces the duration of the process. And for portions of the product weighing up to 5 kg, the required temperature can be achieved even only through machining. The criterion equation of heat transfer to determine the heat transfer coefficient from the wall to the product was obtained by the method of dimensions. A circulation number is entered, which is the ratio of the volume of the circulating product to the volume mixed by the stirrer.

The relative importance of internal and external physical resistances to mass transfer for caffeine release from apple pectin tablets

The relative importance of the physical resistances to mass transfer have been explored by using halved 13 mm diameter apple-pectin tablets containing caffeine, in different external stirring environments within a beaker containing simulated gastric fluid. The effects of different external (outside of the tablets) mass-transfer resistances to the tablets created through two different stirrer types and stirrer speeds, and different internal (inside of the tablets) mass-transfer resistances created through different tablet concentrations and thicknesses, have been studied. These studies enable internal diffusion coefficients of caffeine through the apple pectin matrix to be estimated, as well as estimating the external mass-transfer coefficients from benzoic acid dissolution, which are in the range of 6.5 × 10-6 m/s – 2.4 × 10-5 m/s for the 0.6 mm thick tablets and 4.0 × 10-6 m/s – 1.6 × 10-5 m/s for the 7 mm thick tablets. The diffusion coefficients for different caffeine concentrations in the apple pectin half-tablets have also been calculated in this study. The diffusivity of caffeine in the 7 mm half-tablets with 1% caffeine through 99% pectin was around (1.8 ± 0.5) × 10-10 m2/s. This study points towards the development of multifilm mass-transfer theory for food digestion to create a more fundamentally based understanding of in-vitro digestion systems as an addition to the use of realistic in-vitro food digestion apparatus and give a better correlation between in-vitro and in-vivo digestion tests.

Probing Differences in Mass-Transfer Coefficients in Beaker and Stirrer Digestion Systems and the USP Dissolution Apparatus 2 Using Benzoic Acid Tablets

Measurements of external mass-transfer coefficients for dissolution have been made with benzoic acid tablets with a diameter of 13 mm and approximately 3 mm thick, using two different dissolution systems. One system has been a beaker with a platform for the tablet and either 80 mL or 120 mL of water, with three different types of stirrers, and the other has been a USP dissolution apparatus 2 (paddle) with either 200 mL or 900 mL water. Various stirring speeds have also been used in the different pieces of equipment. The same mass-transfer coefficient may potentially be obtained from the same tablet by adjusting the operating conditions in the two different devices. The ranges of the external mass-transfer coefficients measured in both devices overlapped significantly, with the range being 0.193–4.48 × 10−5 m s−1 in the beaker and stirrer system and 0.222–3.45 × 10−5 m s−1 in the USP dissolution apparatus 2. Dimensional analysis of the results, using Sherwood and Reynolds numbers, shows that the Ranz–Marshall correlation provides a lower bound for estimates of the Sherwood numbers measured experimentally. Calculations of time constants for mass transfer suggest that mass transfer may be a rate-limiting step for dissolution and food digestion under some circumstances. The range of mass-transfer coefficients measured here is representative of other measurements from the literature, and the use of the Ranz–Marshall correlation supports the suggestion that this range of values should be generally expected in most situations.

Batch reactor scale-up of the mixing-sensitive Bechamp reaction based on the heat pulse method

Knowledge and control of mixing in batch processes can prevent yield losses during scale-up. Therefore, in this study, a new heat-mixing model based ono the measurement of the heat distribution after an applied heat pulse, is proposed. The model was developed to predict mesomixing and support scale-up, scale-down, and design and optimisation of batch reactors. The proposed model considers the influences of rotational speed, stirrer type, solvent, stirrer-to-tank diameter, liquid-height-to-tank diameter, injection time, and pumping number. A strong correlation between the mixing time of the heat pulse method and the mass-transfer coefficient of the mixing-sensitive Bechamp reaction was observed.

Simulation of Scale-up Criteria for Side-entry Stirred Tank in Laboratory Scale

The hydrodynamics in side-entry stirred tanks with similar geometry ratio were studied using Computational Fluid Dynamics (CFD) simulation methods. Scale up is done using a flat bottomed cylindrical side-entry stirred tank with diameter D=0.4 m (T40) and D=0.6 m (T60) in a laboratory scale. The type of stirrer is a commercial three-blade marine propeller with a ratio propeller to tank diameter d/D = 0.1. The effect of the constant propeller rotational speed (N) and constant tip speed (utip ) is evaluated on the pumping capacity and fluid velocity profile in the discharge stream area as well as the flow pattern in the whole tank. Flow patterns are a form of fluid behavior that is easily changed when there are operating conditions in the tank varying, for example when the propeller speed is changed. Considered from the effectiveness of mixing performance, the scale-up criteria similar geometry to the constant N is more beneficial. Visually shows that in the same time span the flow pattern on the T60 is more able to reach the entire tank area. The stagnant area is not visible, whereas in T40 there is still a stagnant flow area in the upper left corner of the tank. However, constant N cannot be used as a reference for scale-up of side-entry stirred tank into a larger scale. Because the phenomenon changes quite dramatically which is caused by a change in propeller diameter. Meanwhile constant utip gives results that are closer to T40 and T60 in the flow pattern and the distribution of velocity in the discharge stream. So for side-entry stirred tank that has a similar geometry, scale-up criteria with constant utip is more appropriate to be applied.

PERANCANGAN GEOMETRI DAN POWER PENGADUK UNTUK BIOREAKTOR

Sei Pagar's palm oil mill (PKS Sei Pagar), PTPN V Riau processes fresh fruit bunch into crude palm oil(CPO). This processing also generates waste like empty fruit bunches (EFB), shells, fiber, and palm oilmill effluent (POME). POME has a high content of chemical oxygen demand (COD), approximately30,000-80,000 mg/L, which is usually fermented by bacteria. This fermentation mechanism can beused to produce biogas containing methane in a continuous stirred tank reactor (CSTR). Since POMEor organic materials for biogas production generally contain sludge, the biogas production processshould have an agitator to mix sediment in the base reactor and improve biogas production. Thisresearch aims to determine the agitator's specifications for the biogas pilot plant in PKS Sei Pagar,consisting of power type and type of stirrer include diameter calculation, geometry, and powercalculation. The agitator's power and geometry are determined based on input data from the datasheetreactor and the efficiency of the stirrer is calculated by Reynolds reynolds numbers. From thisresearch's calculations, an agitator geometry for the biogas pilot plant in PKS Sei Pagar had a length of0.875 m, a width of 0.7 m, and a height of 3.5 m. This research also obtained that the motor power resultwas 23.55 HP. The selection of motor power in the Biogas pilot plant's stirring process in PKS Sei Pagarshould have a standard agitator motor power of 25 HP.

Ammonium Fluoroborate Production and Determination of Production Parameters

In this study, the production parameters of ammonium fluoroborate (NH4BF4) synthesis with reaction between boric acid and ammonium hydrogen fluoride were investigated. For this purpose, the effects of parameters such as reactive feeding ratio, reaction temperature, stirring rate, stirrer type, second solvent effect determined separately. Surface morphologies and structural analysis of the crystals obtained after reaction were determined by XRD, FT-IR and SEM analysis respectively. The optimum production conditions were found as reactant feeding rate 1:2, reaction temperature 90 oC, stirring type hot air stirring. Limited oxygen index test results showed that ammonium fluoroborate exhibits excellent flame retardance.

Purification engineering of mono-diacylglycerol using creaming demulsification technique in 20 kg-scale

Glycerolysis is the easiest, cheapest, and most widely used method for producing monodiacylglycerol (MDAG). The crude MDAG resulting from chemical glycerolysis still contains a glycerol residue of more than 7.5% so it needs to be purified. Purification with a simple method using a creaming demulsification technique (CDT) on a laboratory scale has been proven to produce MDAG with a glycerol content of less than 1%. This study was aimed to apply CDT on a scale of 20 kg and determine the process conditions that need to be adjusted so that the results are not different from the laboratory scale. Through trial and error method, the process condition adjustment was done iteratively to produce MDAG glycerol content after purification of less than 1.5%. The initial content of crude MDAG was 12.48%, application of CDT on a scale of 20 kg produces pure MDAG with a glycerol residue content of 3.07% (without adjusting the process conditions) and was 1.15% (with adjusting the process conditions). The adjustments meant include: increasing the operating temperature from 65 to 70°C, changing the type of stirrer from a propeller into a 2-level impeller, applying the nozzle for electrolyte mixing, providing longer skim and cream separation opportunities (applying repeated settling), using 1.5 times more hot water for washing, the washing technique was set twice, the first washing using nozzle without stirring and the second using nozzle with stirring. The adjustments were able to increase the purity of the MDAG produced and has met the European Union and FAO/ WHO standards.

Experimental investigations of Intensity of Mixing of Liquid Media

The constructions of different types of mechanical stirrers are considered and experimental investigations of the process of mixing of viscous liquids are carried out. Dependences of the mixing time on the viscosity of the medium, the modified Reynolds criterion, and the specific mixing power are obtained.

Effect of stirrer design on microstructure of MWCNT and Al alloy by stir casting process

ABSTRACT Composites are proven a better option for automobile, aerospace industry especially due o its specific strength to weight ratio. Aluminium metal matrix composites having its own advantages, stir casting is the most attractive liquid processing method to fabricate the metal matrix composites but the particle distribution inside the matrix is the important concern.. The objective of research work was to investigate the effect of different stirrer design along with bottom pouring technique on the particle distribution in the matrix to prepare a composite. Three different type of stirrer have been designed and used during mixing of reinforcing particles. Composite is prepared via stir casting route with multi walled carbon nano tubes (1.0 wt. %) as reinforcing element and aluminium alloy 6061 as matrix. On investigating the microscopic results, the distribution of reinforcing particles seems uniform and homogeneous with four-bladed disc turbine stirrer compare to others.

Effect of Impeller Design on Power Characteristics and Newtonian Fluids Mixing Efficiency in a Mechanically Agitated Vessel at Low Reynolds Numbers

The mixing process is a widespread phenomenon, which plays an essential role among a large number of industrial processes. The effectiveness of mixing depends on the state of mixed phases, temperature, viscosity and density of liquids, mutual solubility of mixed fluids, type of stirrer, and, what is the most critical property, the shape of the impeller. In the present research, the objective was to investigate the Newtonian fluids flow motion as well as all essential parameters for the mechanically agitated vessel with a new impeller type. The velocity field, the power number, and the pumping capacity values were determined using computer simulation and experimental measurements. The basis for the assessment of the intensity degree and the efficiency of mixing had to do with the analysis of the distribution of velocity vectors and the power number. An experimental and numerical study was carried out for various stirred process parameters and for fluids whose viscosity ranged from low to very high in order to determine optimal conditions for the mixing process.