## 1 Introduction
[15] proposed a simplified design, reducing complexity and improving \begin{table}
\begin{tabular}{c c c c c} \hline \hline
**Type** & **Volume** & **Typical Experimental** & **Level of Monitoring** & **Cost of Operation** \\ \hline  & & throughput & and control & \\ \hline Microtiter plates & 100 \(\mu\)L–3 mL & Very high: thousands & Low: T, biomass, & Medium: capital, increased \\ Small-scale stirred vessels & 10 mL–100 mL & Low/medium: 20 per & product & use of dissolapsules \\  & & technician & product & Low \\ Miniaturized stirred bioreactor & 25 mL–6 L & Medium: 50 mL per & High: PH, oxygen, T, & Medium: capital, labor \\ Shaken vessels & 2 L–50 L & Low: 1–5 technicians & High: pH, oxygen, T, & High: capital, raw \\  & & biomass and product & materials, labor \\ Conventional stirred-tank bioreactor & 1 L–100 L & Low: 1–5 technicians & High: pH, oxygen, T, & High: capital, raw \\ \hline \hline \end{tabular}
\end{table} 
Table 1: Summarized conventional and high-throughput equipment [4; 5; 6; 7]. the accessibility of serviceable parts such as rotating impellers and baffles. [PERSON] and [PERSON] [6] demonstrate adequate performance with regards to measured oxygen transfer capacity values for larger than 500 rpm high shaking frequencies and three and six-millimeter-low shaking diameters, which were conducted in different microtiter plate materials in combination with polystyrene and deionized water. The design of the bioreactor is divided into two aspects, namely, power consumption and mixing efficiency. Power consumption is the most essential significant parameter describing flow regime and mass transfer characteristics in designing and operating bioreactors. The local power consumption of the reactor refers to the external input energy required to keep the fluid motion, and the magnitude of the local power consumption represents the power output of the power system of the reactor in each case. In addition, local power consumption can also reflect the intensity of fluid motion inside the reactor to a certain extent. In general, the more intense the fluid movement, the stronger the material mixing uniformity, but the greater the fluid shear force, increasing the risk of cell death. Therefore, the analysis of the local power consumption of bioreactors can often make a comprehensive analysis of cell growth metabolism problems such as substance mixing and cell damage. The power is transmitted during the shaking process, and different measurement systems are described to determine the average unit volume power (P/V\({}_{\text{L}}\)) of the cylindrical bioreactor. The specific P/V\({}_{\text{L}}\) is one of the basic parameters for microbial process scale-up and scale-down. Parameters that directly affect biological culture, such as oxygen supply, mixing and dispersion of hydraulic stress or organic fluid phases are reliant on specific power inputs [1]. The consequences of changing flask size, shaking frequency and filling volume in relation to observed viscosity change over time during the fermentation process is well documented [15; 16]. During the fermentation process viscosity of the ferment increases, necessitating an increase in power input to maintain consistent mixing [17]. The P/V\({}_{\text{L}}\) values in the cylindrical shaken disposable (single-use) reactor ranged from 0 to 2 kW/m\({}^{3}\) which depend on liquid viscosity, the filling quantity and shaking frequency. [PERSON] et al. [18] introduced current power input correlations as a possible way to describe for the hydrodynamics of the news systems described above. A set of related power-consumption variables is demonstrated with [PERSON]'s \(\pi\)-theorem and converts them to dimensionless Newton numbers. The related numbers are experimentally altered to evaluate the relationship between Reynolds and Froude numbers. A simple correlation is developed for P/V\({}_{\text{L}}\) with seven variables to verify with the 200 L and 2000 L orbitally shaken bioreactors application.